CN105586076A - Crude oil separation method - Google Patents
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Abstract
The invention provides a crude oil separation method including the following steps: 1) performing normal pressure fractionation to the crude oil to obtain normal pressure distillate oil and normal pressure residual oil; 2) feeding the normal pressure residual oil into an extraction column and feeding a main extraction solvent into the middle-lower part of the extraction column so that the normal pressure residual oil is contacted with the main extraction solvent which moves upwardly in a counter-flow manner to obtain a primary extract which moves upwardly to above an inlet of the normal pressure residual oil; 3) enabling the primary extract to pass through at least three temperature gradient zones from bottom to top, in which the temperatures are successively increased from bottom to top, and then arrive to the top of the column; and 4) withdrawing different side-drawn extracts from side-withdrawing lines respectively disposed at the at least three temperature gradient zones and withdrawing a top extract from the column top. By means of the technical scheme, extraction efficiency on the crude oil through solvent extraction is increased and production distribution of the side-drawn extracts from the extraction column is more ideal.
Description
Technical field
The present invention relates to petrochemical industry, particularly, relate to a kind of separation method of crude oil.
Background technology
Along with the development of processing of heavy oil technique, the technology such as coking, hydrogenation (ebullated bed, slurry bubble bed)Adapt to the poor raw material of more character, therefore, how to utilize technique that the light component in crude oil is pulled out,Eating dry bleeding for these devices, is an important problem.
The be otherwise known as time processing of crude oil of atmospheric and vacuum distillation, comprises three operations: the desalination of crude oil, de-Water; Air-distillation; Decompression distillation. Atmospheric and vacuum distillation utilize in crude oil the boiling-point difference between each cut thisCrude oil initial gross separation is become gasoline, kerosene, diesel oil, wax oil and heavy oil by characteristic. Low boiling in crude oilAfter component heating, easily gasify, after high boiling component heating, be difficult for gasification, heating crude oil is arrived to certain temperature,Crude oil partial gasification, is divided into gas-liquid two-phase, contains than low boiling component more in liquid phase in gas phase; WhenWhen product vapour partial condensation, high boiling component is condensation first, and gas-liquid two-phase constantly fully carries out heatExchange and mass exchange, in condensate liquid, heavy constituent constantly increases, and in gas phase, light component constantly increases. OftenDepress, some heavy constituents in crude oil all be gasified, just heating crude oil need to be arrived to higher temperature,But, more than heating crude oil to 350 DEG C time, adopt air-distillation part oil product that cracking will occur existingResemble, oil quality degenerates, oil product generation condensation reaction green coke under high temperature simultaneously, and decompression distillation can be fallenLow oil product boiling point, gasifies it at a lower temperature, and crude oil often decompression is divided into different the heating up in a steamer of boiling spreadPoint, these cut parts are dispatched from the factory with product form after concocting, adding additive, and sizable part isThe raw material of following process device.
Atmospheric and vacuum distillation is to utilize the boiling point difference of each component in crude oil to separate, due in crude oilHigh boiling component is easy cracking in the time of high temperature, and, along with the continuous increase of the degree of depth, vacuum tower are extracted in decompressionEnd temperature raises, and high boiling component cracking degree increases, and the vacuum of vacuum tower is difficult to steady control, because ofThis is difficult to the high boiling component in heavy oil to separate. The vacuum of general decompression distillation reaches700～720mmHg, domestic enterprise is generally the highest at present pulls out 560 DEG C, and abroad some decompressor pulls out621 DEG C, in this case, there are a large amount of heavy constituent generation crackings, cause furnace tubing coking, stoveDuct ligation Jiao not only affects heat transfer, also can stop up so that burn boiler tube, exploding and firing when serious.
The principle of solvent extraction is to utilize the principle of the different solubility of solvent to component in heavy oil to divideFrom, can isolate at low temperatures heavy metal and asphalitine in raw material, thereby obtain high boiling sulfur-bearingOil content, this part of oil content can further be processed into high value-added product, as light Fuel or profitLubricating oil raw material. Solvent extraction is a kind of processing technology that adopts solvent selectivity heavy oil separation, is in essenceThe separation process of liquid-liquid extracting, under certain temperature and pressure, solvent is liquid condition,In extraction tower, feedstock oil (heavy phase) carries out the extracting of liquid liquid with solvent (light phase) counter current contacting from top to bottom,A kind of technique of utilizing physical method to remove the impurity such as fused ring compound in residual oil, metal, sulphur, nitrogenProcess. This technique is not with various hydro carbons, the solubility of non-hydrocarbons material in some low molecular hydrocarbons kind solventsWith as basis, utilize solvent to have large solubility to the aromatic hydrocarbons of alkane-cycloalkane and low condensation, andResin and asphalt is difficult to dissolve or insoluble,practically characteristic, and the solvent that different solvents extracting obtains is taken outCarry oil, at yield with there is qualitatively larger difference, by selective solvent and adjusting process condition, energyAccess the fluid product of the different condition that meets following process. Effect by solvent is this portion in residual oilPoint be difficult to the asphalitine that transforms and fused ring compound and to the harmful heavy metal of catalytic conversion process and sulphur,Nitrogen compound is separated, and using good quality solvent extraction oil as lubricating oil, catalysis and hydrogenationRaw material.
For example, CN102690678A discloses a kind of processing method of heavy crude inferior, specifically openRaw material using the reduced crude of heavy crude inferior as solvent extraction apparatus, warp under supercriticalitySolvent extraction process obtains solvent-refined oil and solvent refining residual oil after processing. But, using the partyWhen method solvent extraction is processed crude oil, the extract extracting single property that derive at extraction tower top, after having limitedThe flexibility of continuous processing.
Summary of the invention
The object of this invention is to provide a kind of separation method of the crude oil with higher extraction efficiency.
To achieve these goals, the invention provides a kind of separation method of crude oil, the method comprises as followsStep: crude oil is carried out normal pressure fractionation by (1), obtains atmospheric distillate and reduced crude; (2) described in inciting somebody to actionReduced crude imports extraction tower, main extraction solvent is imported to the middle and lower part of described extraction tower, makes described normal pressureResidual oil and up described main extraction solvent counter current contacting are carried out extracting, obtain going upward to described reduced crudeThe first extract of entrance top; (3) make described just extract from bottom to up through excess temperature from bottom to topSuccessively rise at least three temperature gradient zones after arrive tower top, on described at least three temperature gradient zones andUnder comprise successively the first temperature gradient zone, the second temperature gradient zone and the 3rd temperature gradient zone; (4) processSide extraction line described in being separately positioned at least three temperature gradient zones is derived respectively different side lines and is taken outExtract, described side is extracted line out and is comprised the first side extraction line, the setting that are arranged at described the first temperature gradient zoneExtract line out and be arranged at the 3rd described temperature gradient zone in the second side of described the second temperature gradient zoneThe 3rd side is extracted line out; Derive tower top extract from described tower top.
By technique scheme, the present invention can improve the extraction efficiency of solvent extraction processing crude oil, takes outThe product of the extract that derive at stripper top distributes more desirable.
Other features and advantages of the present invention are described in detail the detailed description of the invention part subsequently.
Brief description of the drawings
Accompanying drawing is to be used to provide a further understanding of the present invention, and forms a part for description, withDetailed description of the invention one is below used from explanation the present invention, but is not construed as limiting the invention. ?In accompanying drawing:
Fig. 1 is the structural representation of the particularly preferred a kind of embodiment of the present invention device used.
Fig. 2 is the structural representation of the preferred another kind of embodiment of the present invention device used.
Description of reference numerals
1 atmospheric fractional tower 2 extraction towers
3 reduced crude entrance 31 pipelines
32 static mixer 33 pipelines
4 tower tops are extracted line 41 first sides out and are extracted line out
42 second sides are extracted line 43 the 3rd side out and are extracted line out
411 first heat exchanger 421 second heat exchangers
431 the 3rd heat exchanger 441 the 4th heat exchangers
The secondary extraction solvent entrance of 412 first secondary extraction solvent entrance 422 second
432 the 3rd secondary extraction solvent entrance 442 fourth officer extraction solvent entrances
5 main extraction solvent entrance 6 extract remainder outlets
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is elaborated. Should be understood that,Detailed description of the invention described herein only, for description and interpretation the present invention, is not limited to the present invention.
In the present invention, in the situation that not doing contrary explanation, the noun of locality of use as " upper and lower, the end,Top " normally undefined in the normal situation about using of the present invention's device used, particularly can reference diagramPage shown in 1, " inside and outside " refers to the interior and outer of respective profile. It should be noted that, theseThe noun of locality, only for the present invention is described, is not limited to the present invention.
The invention provides a kind of separation method of crude oil, the method comprises the steps: that (1) is by crude oilCarry out normal pressure fractionation, obtain atmospheric distillate and reduced crude; (2) described reduced crude is imported to extractingTower, imports main extraction solvent the middle and lower part of described extraction tower, make described reduced crude and up described inMain extraction solvent counter current contacting is carried out extracting, obtains first the taking out of the entrance top that goes upward to described reduced crudeExtract; (3) make that described just extract rises successively through excess temperature from bottom to up from bottom to top at least threeBehind individual temperature gradient zone, arrive tower top, described at least three temperature gradient zones comprise first from top to bottom successivelyTemperature gradient zone, the second temperature gradient zone and the 3rd temperature gradient zone; (4) described in process is separately positioned onSide at least three temperature gradient zones is extracted line out and is derived respectively different side line extracts, and described side is extracted outLine comprise be arranged at described the first temperature gradient zone first side extract out line, be arranged at described the second temperature ladderSecond side in degree district is extracted line out and is arranged at the 3rd side extraction line of the 3rd described temperature gradient zone; From instituteState tower top and derive tower top extract.
Wherein, crude oil is carried out to the device of normal pressure fractionation and operation can be according to petrochemical industry routineMode is carried out, and person skilled in art knows this, and the present invention does not repeat them here. Wherein, described inReduced crude refers to the cut of boiling range more than 350 DEG C.
According to separation method of the present invention, wherein, the minimum temperature of the temperature of described tower top is than described firstThe high 1-8 DEG C of temperature gradient zone maximum temperature, preferred high 1.5-5 DEG C. In described the first temperature gradient zoneLow temperature is than the high 2-15 DEG C of the maximum temperature of described the second temperature gradient zone, preferred high 2-10 DEG C; DescribedMinimum temperature in two temperature gradient zones is than the high 3-25 DEG C of the maximum temperature of described the 3rd temperature gradient zone, excellentSelect high 3-18 DEG C;
According to separation method of the present invention, wherein, the maximum temperature of each temperature gradient zone and minimum temperatureCan be identical, preferably, wherein, the maximum temperature in described the first temperature gradient zone is than described the first temperatureThe high 0.1-3 DEG C of minimum temperature of degree gradient zones, preferred high 0.2-2 DEG C; In described the second temperature gradient zoneMaximum temperature is than the high 0.1-5 DEG C of the minimum temperature of described the second temperature gradient zone, preferred high 0.2-3 DEG C; InstituteState maximum temperature in the 3rd temperature gradient zone higher than the minimum temperature of described the 3rd temperature gradient zone0.1-8 DEG C, preferred high 0.2-6 DEG C.
According to separation method of the present invention, wherein, the pressure of described tower can be 0.5-5MPa, is preferably1-4MPa, tower top temperature can be 100-300 DEG C, is preferably 120-280 DEG C. According to of the present invention pointFrom method, wherein, the temperature at the bottom of the tower of described extraction tower can be 90-290 DEG C, is preferably 100-270 DEG C.
According to separation method of the present invention, wherein, with respect to the described tower top extracting of 1 weight portion of extracting outThing, the first extract of extracting line extraction through described the first side out can be 1-4 weight portion, is preferably 2-3Weight portion, the second extract of extracting line extraction through described the second side out can be 1-4 weight portion, is preferably2-3 weight portion, the 3rd extract of extracting line extraction through described the 3rd side out can be 1-4 weight portion, excellentElect 2-3 weight portion as. Wherein, in order to maintain the continuous operation of extraction tower, preferably, logical in extraction towerThe mass flow entering and the mass flow of extraction form balance. Tower top is extracted oil out can derive dress as requiredPut or partly circulate as overhead reflux.
According to separation method of the present invention, wherein, the volume of described main extraction solvent and described reduced crudeThan can be (1-15): 1; Be preferably (2-13): 1, more preferably (3-10): 1.
According to separation method of the present invention, wherein, described main extraction solvent contains that to have 4-11 carbon formerAt least one in the petroleum solvents such as hydrocarbon, naphtha and the benzinum of son. Preferably, described main extracting is moltenAgent can contain the hydrocarbon with 4-11 carbon atom, and for example, described main extraction solvent can comprise but not limitAt least one in normal butane, iso-butane, pentane, isopentane, hexane, heptane and octane. MorePreferably, described main extraction solvent comprises at least one in normal butane, iso-butane, pentane, isopentaneKind. Preferably, described main extraction solvent can be also naphtha and/or benzinum.
A preferred embodiment of the invention, the method can also comprise: at described at least threeHeat exchanger is set respectively in temperature gradient zone and carries out heat exchange, with at least three thermogrades described in maintaining respectivelyDistrict's temperature separately. Wherein, in described heat exchanger, can pass into conduction oil and heat, or by electricityHeat heating.
According to another kind of preferred embodiment of the present invention, the method also comprises: to described at least three temperatureDegree passes into respectively the secondary extraction solvent of preheating in gradient zones, with at least three thermogrades described in maintaining respectivelyDistrict's temperature separately. Wherein, the temperature of the secondary extraction solvent of preheating can be adjusted as required.
Wherein, in order to reduce the difficulty of removing solvent, preferably, described secondary extraction solvent and described master take outThe composition of extraction solvent is identical; And the gross weight of described secondary extraction solvent and the volume of described main extraction solventRatio is 1:(1-15), more preferably 1:(1-12).
According to separation method of the present invention, wherein, in the embodiment of secondary extraction solvent that passes into preheating,The consumption of described main extraction solvent can reduce, for example, and the volume of described main extraction solvent and described normal pressureThe volume ratio of residual oil can be (1-10): 1.
According to separation method of the present invention, wherein, in order to increase the extracting time of contact to reduced crude,Preferably, the method also comprises: by mixed through static mixer to described reduced crude and premix extraction solventAfter closing, mix rear importing extraction tower. Described static mixer can have 2-5, and goes here and there successivelyConnection. Between preferably in described each static mixer, all can inject one pre-miscible agent.
According to separation method of the present invention, wherein, preferably, described premix extraction solvent and described master take outThe composition of extraction solvent is identical; The pre-miscible agent injecting between described each static mixer and described master take outThe volume ratio of extraction solvent is 1:(1-15), be preferably 1:(1-12), more preferably 1:(1-10).
According to separation method of the present invention, wherein, described reduced crude and premix extraction solvent are being carried outIn mixed preferred embodiment, the consumption of described main extraction solvent can reduce, for example, described normalPressing the volume ratio of residual oil and described main extraction solvent can be 1:(1-7).
According to separation method of the present invention, the solvent-refined oil that extracting obtains can enter and urge according to its characterChange cracking or hydrogenation plant, the tailings at the bottom of extraction tower can be directly as slurry bubble bed hydrogenating materials, cokingRaw material, gasified raw material, boiler oil or mixing asphalt component etc.
Below, further describe the present invention by embodiment. In following examples, No. 1 usedCrude oil and No. 2 former oil properties (detecting according to the method in national standard and professional standard) are as tableShown in 1.
Table 1
| Crude title | No. 1 crude oil | No. 2 crude oil |
| 20 DEG C of density, g/cm3 | 0.9051 | 0.8481 |
| 50 DEG C of viscosity, mm2/s | 28.38 | 5.37 |
| Condensation point, DEG C | -20 | -28 |
| Carbon residue, m% | 8.70 | 2.98 |
| Acid number, mgKOH/g | 1.44 | 0.12 |
| Salt content, mgNaCl/L | 1982 | 42 |
| C,m％ | 85.58 | 85.41 |
| H，m％ | 12.19 | 13.19 |
| S,m％ | 1.46 | 0.78 |
| N,m％ | 0.20 | 0.13 |
| Ni,ppm | 12.2 | 3.4 |
| V,ppm | 76.3 | 21.0 |
Embodiment 1
No. 1 crude oil and No. 2 crude oil are carried out to normal pressure fractionation, obtain respectively No. 1 atmospheric distillate and No. 1Reduced crude and No. 2 atmospheric distillates and No. 2 reduced crudes; In national standard and professional standardMethod detect, the character of No. 1 reduced crude and No. 2 reduced crudes is as shown in table 2.
Table 2
| Crude title | No. 1 reduced crude | No. 2 reduced crudes |
| Yield, m% | 69.81 | 55.58 |
| 20 DEG C of density, g/cm3 | 0.9697 | 0.9331 |
| 100 DEG C of viscosity, mm2/s | 110.2 | 25.43 |
| Carbon residue, m% | 13.2 | 6.35 |
| H,m％ | 11.35 | 12.13 |
| S,m％ | 2.21 | 1.54 |
| Ni,ppm | 29.2 | 10.2 |
| V,ppm | 173 | 49.0 |
| Saturated point, m% | 40.8 | 54.8 |
| Fragrance point, m% | 33.3 | 33.7 |
| Colloid, m% | 19.0 | 10.7 |
| Asphalitine, m% | 6.9 | 0.8 |
Embodiment 2
After mixing with premix extraction solvent, No. 1 reduced crude that embodiment 1 is obtained imports extraction tower, and willMain extraction solvent imports the middle and lower part of described extraction tower, makes described reduced crude and up described main extractingSolvent counter current contacting is carried out extracting, obtains the first extract of the entrance top that goes upward to described reduced crude,No. 1 reduced crude is entered and is taken out by three static mixers sequentially with after three bursts of premix solventStripper. Wherein, the weight ratio of No. 1 reduced crude and main extraction solvent and premix extraction solvent is 1:7:5. Wherein, main extraction solvent and premix extraction solvent are naphtha.
Make described the 3rd temperature ladder that just extract rises successively through excess temperature from bottom to up from bottom to topDegree district, the second temperature gradient zone and the first temperature gradient zone; The highest temperature in described the first temperature gradient zoneDegree is 263 DEG C, and minimum temperature is 261 DEG C; Maximum temperature in described the second temperature gradient zone is 255 DEG C,Minimum temperature is 252 DEG C; Maximum temperature in described the 3rd temperature gradient zone is 245 DEG C, minimum temperatureBe 240 DEG C, the temperature of tower top is 268 DEG C. The pressure of tower top is 3MPa. Temperature at the bottom of tower is 220 DEG C.Wherein, in described the first temperature gradient zone, the second temperature gradient zone and the 3rd temperature gradient zone, arrange respectivelyThere is heat exchanger to carry out heat exchange, to maintain respectively their temperature.
Derive respectively different sides through the side extraction line being separately positioned in above-mentioned three temperature gradient zonesLine extract, described side extract out line comprise the first side that is arranged at described the first temperature gradient zone extract out line,The second side that is arranged at described the second temperature gradient zone is extracted line out and is arranged at the 3rd described thermogradeThe 3rd side in district is extracted line out; Derive tower top extract from described tower top. Wherein, with respect to 1 weight of extracting outThe described tower top extract of amount part, the first extract of extracting line extraction through described the first side out is 2 weight portions,The second extract of extracting line extraction through described the second side out is 2.5 weight portions, extracts line out through described the 3rd sideThe 3rd extract of extracting out is 3 weight portions.
By described tower top extract, described the first extract, described the second extract and described the 3rd extractingExtraction solvent in thing is removed respectively and reuse, obtains tower top refined oil, the first refined oil, second refiningOil and the 3rd refined oil. The character that detects them according to national standard and professional standard, result is as table 3Show.
Table 3
Embodiment 3
No. 1 reduced crude that embodiment 1 is obtained mix with premix extraction solvent after import extraction tower inTop, imports main extraction solvent the middle and lower part of described extraction tower, makes described reduced crude and up instituteState main extraction solvent counter current contacting and carry out extracting, obtain going upward to described reduced crude entrance top at the beginning ofExtract. Wherein, No. 1 reduced crude sequentially with three bursts of premix solvent after quiet by threeState blender enters extraction tower. The weight ratio of No. 1 reduced crude and main extraction solvent and premix extraction solventFor 1:7:5. Wherein, main extraction solvent and premix extraction solvent are naphtha.
Make described the 3rd temperature ladder that just extract rises successively through excess temperature from bottom to up from bottom to topDegree district, the second temperature gradient zone and the first temperature gradient zone; The highest temperature in described the first temperature gradient zoneDegree is 263 DEG C, and minimum temperature is 261 DEG C; Maximum temperature in described the second temperature gradient zone is 255 DEG C,Minimum temperature is 252 DEG C; Maximum temperature in described the 3rd temperature gradient zone is 245 DEG C, minimum temperatureBe 240 DEG C, the temperature of tower top is 268 DEG C. The pressure of tower top is 3MPa. Temperature at the bottom of tower is 220 DEG C.Wherein, in the first temperature gradient zone, the second temperature gradient zone and the 3rd temperature gradient zone, pass into respectively in advanceThe secondary extraction solvent of heat, to maintain respectively their temperature separately. Particularly, to the first temperature gradient zoneThe temperature that passes into the secondary extraction solvent of preheating is 262 DEG C, the ratio of intake and the weight of No. 1 reduced crudeValue is 0.3:1; The temperature that passes into the secondary extraction solvent of preheating to the second temperature gradient zone is 254 DEG C, logicalThe ratio that enters the weight of amount and No. 1 reduced crude is 0.5:1; Pass into preheating to the 3rd temperature gradient zoneThe temperature of secondary extraction solvent is 243 DEG C, and the ratio of the weight of intake and No. 1 reduced crude is 1:1.Shown in secondary extracting be naphtha.
Derive respectively different sides through the side extraction line being separately positioned in above-mentioned three temperature gradient zonesLine extract, described side extract out line comprise the first side that is arranged at described the first temperature gradient zone extract out line,The second side that is arranged at described the second temperature gradient zone is extracted line out and is arranged at the 3rd described thermogradeThe 3rd side in district is extracted line out; Derive tower top extract from described tower top. Wherein, with respect to 1 weight of extracting outThe described tower top extract of amount part, the first extract of extracting line extraction through described the first side out is 2 weight portions,The second extract of extracting line extraction through described the second side out is 2.5 weight portions, extracts line out through described the 3rd sideThe 3rd extract of extracting out is 3 weight portions.
By described tower top extract, described the first extract, described the second extract and described the 3rd extractingExtraction solvent in thing is removed respectively and reuse, obtains tower top refined oil, the first refined oil, second refiningOil and the 3rd refined oil. The character that detects them according to national standard and professional standard, result is as table 4Show.
Table 4
Embodiment 4
Carry out the separation of reduced crude according to the method for embodiment 2, different, the reduced crude of useNo. 2 reduced crudes that obtain for embodiment 1.
According to national standard and professional standard detect tower top refined oil, the first refined oil, the second refined oil andThe 3rd refining oil properties, result is as shown in table 5.
Table 5
Embodiment 5
Carry out the separation of reduced crude according to the method for embodiment 3, different, the reduced crude of useNo. 2 reduced crudes that obtain for embodiment 1.
According to national standard and professional standard detect tower top refined oil, the first refined oil, the second refined oil andThe 3rd refining oil properties, result is as shown in table 6.
Table 6
Comparative example 1
Method according to embodiment 2 separates reduced crude, different, the first temperature gradient zone,The temperature of the second temperature gradient zone and the 3rd temperature gradient zone is basic identical, is 278 DEG C, does not use and changesHot device is controlled the temperature in the first temperature gradient zone, the second temperature gradient zone and the 3rd temperature gradient zoneSystem.
According to national standard and professional standard detect tower top refined oil, the first refined oil, the second refined oil andThe 3rd refining oil properties, result is as shown in table 7.
Table 7
Can find out according to the contrast of embodiment 2 and comparative example 1, former oil separating method of the present invention canImprove solvent extraction and process the extraction efficiency of crude oil, and the product of the extract of extraction tower top derivation distributesMore desirable.
Comparative example 2
As different from Example 1, the reduced crude that identical raw material obtains after air-distillation entersRow decompression distillation, decompression distillation cutting temperature is 524 DEG C, vacuum distillate yield is only 52.2, and characterApproach with solvent-refined oil. And the operating temperature in vacuum distillation process is far above the operation of solvent extractionTemperature, because raw material is heavier, can find, wayward in operating process, raw material is in decompression distillationIn journey, there is partial cracking and condensation, at the bottom of still, have coking material to generate.
Below describe by reference to the accompanying drawings the preferred embodiment of the present invention in detail, still, the present invention does not limitDetail in above-mentioned embodiment, within the scope of technical conceive of the present invention, can be to the present inventionTechnical scheme carry out multiple simple variant, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each the concrete technical characterictic described in above-mentioned detailed description of the invention,In reconcilable situation, can combine by any suitable mode, for fear of unnecessaryRepeat, the present invention is to the explanation no longer separately of various possible combinations.
In addition, between various embodiment of the present invention, also can be combined, as long as itsWithout prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (17)
1. a separation method for crude oil, is characterized in that: the method comprises the steps:
(1) crude oil is carried out to normal pressure fractionation, obtain atmospheric distillate and reduced crude;
(2) by the middle and upper part of described reduced crude importing extraction tower, main extraction solvent is imported to described extraction tower, make described reduced crude and up described main extraction solvent counter current contacting carry out extracting, obtain the first extract of the entrance top that goes upward to described reduced crude;
(3) make to arrive tower top behind described just at least three temperature gradient zones that extract rises successively through excess temperature from bottom to up from bottom to top, described at least three temperature gradient zones comprise the first temperature gradient zone, the second temperature gradient zone and the 3rd temperature gradient zone from top to bottom successively;
(4) extract line out through the side at least three temperature gradient zones described in being separately positioned on and derive respectively different side line extracts, described side is extracted the 3rd side that line comprises that the first side that is arranged at described the first temperature gradient zone is extracted line out, the second side of being arranged at described the second temperature gradient zone is extracted line out and be arranged at the 3rd described temperature gradient zone out and is extracted line out; Derive tower top extract from described tower top.
2. separation method according to claim 1, is characterized in that: the minimum temperature of the temperature of described tower top is than the high 1-8 DEG C of described the first temperature gradient zone maximum temperature; Minimum temperature in described the first temperature gradient zone is than the high 2-15 DEG C of the maximum temperature of described the second temperature gradient zone; Minimum temperature in described the second temperature gradient zone is than the high 3-25 DEG C of the maximum temperature of described the 3rd temperature gradient zone.
3. separation method according to claim 1 and 2, is characterized in that: the maximum temperature in described the first temperature gradient zone is than the high 0.1-3 DEG C of the minimum temperature of described the first temperature gradient zone; Maximum temperature in described the second temperature gradient zone is than the high 0.1-5 DEG C of the minimum temperature of described the second temperature gradient zone; Maximum temperature in described the 3rd temperature gradient zone is than the high 0.1-8 DEG C of the minimum temperature of described the 3rd temperature gradient zone.
4. separation method according to claim 1 and 2, is characterized in that: the pressure of described extraction tower is 0.5-5MPa, and extracting tower top temperature is 100-300 DEG C.
5. separation method according to claim 4, is characterized in that: the temperature at the bottom of the tower of described extraction tower is 90-290 DEG C.
6. separation method according to claim 1 and 2, it is characterized in that: with respect to the described tower top extract of 1 weight portion of extracting out, the first extract of extracting line extraction through described the first side out is 1-4 weight portion, the second extract of extracting line extraction through described the second side out is 1-4 weight portion, and the 3rd extract of extracting line extraction through described the 3rd side out is 1-4 weight portion.
7. separation method according to claim 1, is characterized in that: the volume ratio of described main extraction solvent and described reduced crude is (1-15): 1.
8. according to the separation method described in claim 1 or 7, it is characterized in that: described main extraction solvent contains at least one in hydrocarbon, naphtha and the benzinum with 4-11 carbon atom.
9. separation method according to claim 1 and 2, is characterized in that: the method also comprises: in described at least three temperature gradient zones, heat exchanger is set respectively and carries out heat exchange, with the temperature separately of at least three temperature gradient zones described in maintaining respectively.
10. separation method according to claim 1 and 2, is characterized in that: the method also comprises: to the secondary extraction solvent that passes into respectively preheating in described at least three temperature gradient zones, with the temperature separately of at least three temperature gradient zones described in maintaining respectively.
11. separation methods according to claim 10, is characterized in that: described secondary extraction solvent is identical with the composition of described main extraction solvent; And the ratio of the gross weight of described secondary extraction solvent and the weight of described main extraction solvent is 1:(1-15).
12. separation methods according to claim 11, is characterized in that: the volume of described main extraction solvent and the volume ratio of described reduced crude can be (1-10): 1.
13. separation methods according to claim 1 and 2, is characterized in that: the method also comprises: described reduced crude is imported to extraction tower with premix extraction solvent after static mixer mixes.
14. separation methods according to claim 13, is characterized in that: described static mixer has 2-5, and series connection successively.
15. separation methods according to claim 14, is characterized in that, all can inject one pre-miscible agent between in described each static mixer.
16. according to the separation method described in right 15, it is characterized in that, the volume ratio of the pre-miscible agent injecting between described each static mixer and described main extraction solvent is 1:(1-15).
17. separation methods according to claim 13, is characterized in that: the weight ratio of described reduced crude and described main extraction solvent is 1:(1-7).
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| CN102643669A (en) * | 2011-02-21 | 2012-08-22 | 中国石油化工股份有限公司 | A production method of low density environment-friendly rubber filling oil |
| CN102690678A (en) * | 2011-03-24 | 2012-09-26 | 中国石油化工股份有限公司 | Processing method of inferior heavy crude oil |
| CN103059921A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Heavy oil separation method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102643669A (en) * | 2011-02-21 | 2012-08-22 | 中国石油化工股份有限公司 | A production method of low density environment-friendly rubber filling oil |
| CN102690678A (en) * | 2011-03-24 | 2012-09-26 | 中国石油化工股份有限公司 | Processing method of inferior heavy crude oil |
| CN103059921A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Heavy oil separation method |
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