CN105586069A - A solvent extraction method - Google Patents
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- CN105586069A CN105586069A CN201410569449.XA CN201410569449A CN105586069A CN 105586069 A CN105586069 A CN 105586069A CN 201410569449 A CN201410569449 A CN 201410569449A CN 105586069 A CN105586069 A CN 105586069A
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Abstract
An extraction device is disclosed. The extraction device comprises an extraction column, at least one extract outlet, at least one extracting solvent inlet and at least one raffinate outlet, wherein the at least one extract outlet, the at least one extracting solvent inlet and the at least one raffinate outlet are disposed in the extraction column in order from top to bottom. At least two feeding ports are disposed between the extract outlet and the extracting solvent inlet of the extraction column and comprise a first feeding port and a second feeding port. The height difference between the first feeding port and the extracting solvent inlet is larger than the height difference between the second feeding port and the extracting solvent inlet. A method for treating heavy oil is also disclosed. The heavy oil comprises first raw material oil and second raw material oil which are independent and orderly reduced in relative density. The method includes feeding an extracting solvent to the lower part of the extraction device, feeding the heavy oil into the middle and upper parts of the extraction device, and performing extraction with the heavy oil being in countercurrent contact with the rising extracting solvent. By the technical scheme, the extraction efficiency for treating the heavy oil is effectively increased.
Description
Technical field
The present invention relates to petrochemical industry, particularly, relate to a kind of extraction equipment and a kind of heavy of processingThe method of oil.
Background technology
Solvent extraction process can be isolated heavy metal and the asphalitine in raw material at low temperatures, in crude oil dayToday of the in poor quality that becomes, solvent extraction technology has clear superiority in oil plant processing technology. Solvent extractionGetting is the separation process (being also referred to as extractive process) of a liquid-liquid extraction in essence, in certain temperatureUnder pressure, solvent is liquid condition, in extraction tower, feedstock oil (heavy phase) from top to bottom with solvent(light phase) counter current contacting is carried out liquid-liquid extraction, is that a kind of to utilize physical method to remove pitch in residual oil thickThe technical process of the impurity such as cycle compound, metal, sulphur, nitrogen. This technique is with various hydro carbons, non-hydrocarbons thingThe different solubility of matter in some low molecular hydrocarbons kind solvents, as basis, utilizes solvent to alkane-cycloalkanesThe aromatic hydrocarbons of hydrocarbon and low condensation has large solubility, and resin and asphalt is difficult to dissolving or almost insolubleCharacteristic, different solvents extracts the deasphalted oil obtaining, at yield with there is qualitatively a larger difference,By selective solvent and adjusting process condition, the liquid that can be met the different condition of following process producesProduct. Effect by solvent in decompression residuum this part be difficult to asphalitine of transforming and fused ring compound withAnd the harmful heavy metal of catalytic conversion process and sulphur, nitrogen compound are separated, and quality is goodDeasphalted oil is as the raw material of lubricating oil, catalytic cracking and hydrotreatment/cracking. Its general principle is to utilizeThe difference of the solubility of solvent to the each component of oil phase, is not distributed in two liquid phases, then them equallyBy the separation of two liquid phases, realize the separation between component, in extraction process, oil phase and solvent are in extraction towerClose contact, allows oil phase enter in solvent agent by interface, phase border, until each component is in two alternate distributionSubstantially reach balance. Then by sedimentation, be separated into two-layer liquid, by solvent-refined oil and refining, when extraction reaches while balancing each other, there are two alternate distribution coefficients in residual solution.
Extraction tower is the key equipment of solvent extraction technology, and solvent extraction is at present conventional two kinds: it is heavy to mixFormula extractor, counter-current extraction tower fall. The separating effect of counter-current extraction tower is than the extraction of single hop mixing-decanter typeGetting the separating effect of device will get well. In counter-current extraction tower, lightweight solvent enters from the bottom of tower, is continuousUpper flowing in opposite directions. Residual oil enters from the top of tower, relies on gravity downwards by the solvent of continuous phase. At slagFluid drips in the process of downward sedimentation, and the aromatic hydrocarbons of alkane-cycloalkane and low condensation etc. is dissolved in solvent,And resin and asphalt is precipitated. Finally, drop is gathered in the bottom of tower, as de-oiled asphalt from towerExtract out bottom. The continuous phase solvent that contains deasphalted oil is heated at the top of tower, makes the large molecule of a partAromatic hydrocarbons from solution, separate. These macromolecular aromatic hydrocarbons flow downward by solvent layer, play backThe effect of stream, has improved separating effect.
Document " research of the efficient extraction tower of solvent deasphalting and application " and " solvent deasphalting efficiently extractsGet the application of tower " be mainly, based on hydrodynamics, extraction tower extraction efficiency has been carried out to analysis and modification, butBe mainly for be the work that the filler of extraction tower is carried out, instead of grind from the angle of liquid-liquid extractionStudy carefully.
Solvent-extracted extraction tower is divided into several regions, and each region has it specifically to act on, foot oneAs the decanting zone of heavy constituent; Near colvent inlet, be bitumen and scrubbing section, have there freshSolvent injects the heavy constituent with washing coagulation, and the oil content that makes to be adsorbed in heavy constituent is further separated;At solvent and this interval of raw material residual oil entrance, the oil content of needs is dissolved out, and is rich in asphalitine or glueThe heavy constituent of matter is precipitated; Part more than feedstock oil entrance is the decanting zone of deasphalted oil, and it shows classThe effect of pseudoselectivity solvent, further removes the undesirable components being dissolved in depitching solution,To ensure deasphalted oil quality, the main matter that relies on the process adjustments deasphalted oil that adopts one section or two sectionsAmount, still, adopts in this way the not characteristic of the raw material of foundation processing, increases to a great extentEnergy consumption.
The mode of in existing solvent extraction technology, feedstock oil being entered to extraction tower is the middle and upper part by extraction towerFixed position enters, but production practices prove, there is extraction efficiency in existing solvent extraction technology methodLower defect.
Summary of the invention
The object of the invention is to overcome the defect that extraction efficiency is lower, the extraction that a kind of extraction efficiency is higher is providedGet the method for the processing mink cell focus that device and a kind of extraction efficiency are higher.
The present inventor finds, if it is different to pass into relative density at the differing heights place of extraction towerFeedstock oil, can improve extraction efficiency, has obtained thus the present invention.
To achieve these goals, the invention provides a kind of extraction equipment, this extraction equipment comprises extractionTower and be successively set on from top to bottom the outlet of at least one extract, at least one extraction on extraction towerSolvent inlet and the outlet of at least one raffinate; Described extract outlet and described extraction at extraction tower are moltenBetween agent import, be provided with at least two feed entrances, described at least two feed entrances comprise that first entersMaterial entrance and the second feed entrance; And the height between described the first feed entrance and described extractant importThe poor difference in height being greater than between described the second feed entrance and described extractant import of degree.
To achieve these goals, the present invention also provides a kind of method of processing mink cell focus, described heavyOil comprises independence and at least two kinds of different feedstock oils of relative density, and the method comprises extractant is passed intoThe bottom of extraction equipment, passes into described mink cell focus the middle and upper part of extraction equipment, makes described mink cell focus and upperThe described extractant counter current contacting of row extracts; Described extraction equipment comprise extraction tower and from upper toUnder be successively set on the outlet of at least one extract, at least one the extractant import on described extraction towerWith at least one raffinate outlet; Between described extract outlet and described extractant import, arrangeThere are at least two feed entrances; Described at least two feed entrances comprise the first feed entrance and the second chargingEntrance, and difference in height between described the first feed entrance and described extractant import is greater than described secondDifference in height between feed entrance and described extractant import; Wherein, described the first feed entrance passes intoThe feedstock oil that relative density is high, described the second feed entrance passes into the feedstock oil that described relative density is low.
To achieve these goals, the present invention also provides a kind of method of processing mink cell focus, described heavyThe first feedstock oil that comprise oil independence and relative density reduce successively and the 3rd feedstock oil, the method comprise byExtractant passes into the bottom of extraction equipment, described mink cell focus is passed into the middle and upper part of extraction equipment, makes instituteStating mink cell focus and up described extractant counter current contacting extracts; Described extraction equipment comprises extractionTower and be successively set on from top to bottom at least one extract outlet on described extraction tower, at least oneExtractant import and the outlet of at least one raffinate; Enter in described extract outlet and described extractantBetween mouthful, be provided with at least two feed entrances; Described at least two feed entrances comprise that first is fed intoMouthful and the 3rd feed entrance, and difference in height between described the first feed entrance and described extractant importBe greater than the difference in height between described the 3rd feed entrance and described extractant import; Wherein, by describedOne feedstock oil passes into described the first feed entrance, and described the 3rd feedstock oil is passed into described the 3rd feed entrance.
By technique scheme, the present invention can improve the extraction efficiency of processing mink cell focus effectively.
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 extraction equipment of the particularly preferred a kind of embodiment of the present invention.
Fig. 2 is the structural representation of the extraction equipment of the preferred another kind of embodiment of the present invention.
Description of reference numerals
1 first feed entrance 11 first feed distributors
111 first fillers
2 second feed entrance 21 second feed distributors
211 second fillers
3 the 3rd feed entrance 31 the 3rd feed distributors
311 the 3rd fillers
4 extracts export 6 extraction towers
7 extractant import 71 extractant distributors
8 raffinates export 9 heaters
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 device provided by the invention, particularly can reference diagramPage shown in 1, " inside and outside " refers to the interior and outer of respective profile; The liquid using or gasVolume numerical value is 20 DEG C and 1 numerical value that normal atmosphere is depressed.
The invention provides a kind of extraction equipment, this extraction equipment comprises extraction tower 6 and complies with from top to bottomInferior at least one extract outlet 4, at least one extractant import 7 being arranged on described extraction towerWith at least one raffinate outlet 8; At described extract outlet 4 and the described extractant of extraction tower 6Between import 7, be provided with at least two feed entrances, described at least two feed entrances comprise that first entersMaterial entrance 1 and the second feed entrance 2; And described the first feed entrance 1 and described extractant import 7Between difference in height be greater than the difference in height between described the second feed entrance 2 and described extractant import 7.
Wherein, described extraction tower 6 can be counter-current extraction tower; Tower height and the tower diameter of described extraction tower 6 canThink the selection of solvent deasphalting field routine, for example tower height can be 15-40 rice, and tower diameter can be 1-5Rice.
Wherein, the difference in height between described the first feed entrance 1 and described extractant import 7 is greater than instituteState the height between the second feed entrance 2 and described extractant import 7, for example described first entersDifference in height between material entrance 1 and described extractant import 7 with respect to described the second feed entrance 2 andThe ratio of the difference in height between described extractant import 7 can be (1.03-1.5): 1, be preferably(1.05-1.3)：1。
Wherein, as one of the present invention preferred embodiment, described at least two feed entrances also compriseThe 3rd feed entrance 3; And the height between described the second feed entrance 2 and described extractant import 7The poor difference in height being greater than between described the 3rd feed entrance 3 and described extractant import 7.
Wherein, the difference in height between described the first feed entrance 1 and described extractant import 7 with respect toThe ratio of the difference in height between described the second feed entrance 2 and described extractant import 7 can be(1.03-1.5): 1, be preferably (1.05-1.3): 1; Described the second feed entrance 2 is molten with described extractionDifference in height between agent import 7 with respect to described the 3rd feed entrance 3 and described extractant import 7 itBetween the ratio of difference in height can be (1.03-1.5): 1, be preferably (1.05-1.3): 1.
Wherein, described feed entrance is connected with or is not connected with the charging distribution being placed in extraction tower independentlyDevice. Preferably, the first feed entrance 1 is connected with the first feed distributor 11 being placed in extraction tower;The second feed entrance 2 is connected with the first feed distributor 21 being placed in extraction tower; The 3rd feed entrance 3Be connected with the first feed distributor 31 being placed in extraction tower.
Wherein, between described feed entrance and described extractant import (7), can be provided with and be placed in extractionGet at least one in sieve plate, rotating disk and the filler in tower. Preferably, as Fig. 1 institute formula, the 3rd chargingBetween entrance 3 and extractant import 7, be provided with the 3rd filler 311. Preferably, as shown in Figure 2,Between the second feed entrance 2 and extractant import 7, be provided with the second filler 211
Wherein, between at least one pair of adjacent described feed entrance, can be provided with sieve plate, rotating disk and fillerIn at least one. Preferably, as shown in Figure 1, in extraction tower 6, the first feed entrance 1 andBetween two feed entrances 2, can be provided with the first filler 111; The second feed entrance 2 and the 3rd is fed intoBetween mouth 3, be provided with the second filler 211. Preferably, as shown in Figure 2, in extraction tower 6, firstBetween feed entrance 1 and the second feed entrance 2, can be provided with the first filler 111.
Wherein, as the particularly preferred a kind of embodiment of the present invention, described at least two feed entrance bagsDraw together the first feed entrance 1 and the second feed entrance 2; Described the first feed entrance 1 and described extractantDifference in height between import 7 is with respect between described the second feed entrance 2 and described extractant import 7The ratio of difference in height be (1.2-1.3): 1; In described the first feed entrance 1, being connected with the first charging dividesCloth device 11; In described the second feed entrance 2, be connected with the second feed distributor 21; Described the first chargingBetween entrance 1 and described the second feed entrance 2, be provided with at least one in sieve plate, rotating disk and filler.In this preferred embodiment, extraction equipment of the present invention is particularly suitable for carrying out to comprising independent and relatively closeThe first feedstock oil that degree reduces successively and the described feedstock oil of the 3rd feedstock oil extract; Wherein saidOne feedstock oil is 1-1.2g/mL the relative density of 20 DEG C, relatively close at 20 DEG C of described the 3rd feedstock oilDegree 0.9 to being less than 0.9340g/mL, for example, is 0.9-0.9335g/mL.
Wherein, as the particularly preferred a kind of embodiment of the present invention, described at least two feed entrance bagsDraw together the first feed entrance 1 and the second feed entrance 2; Described the first feed entrance 1 and described extractantDifference in height between import 7 is with respect between described the second feed entrance 2 and described extractant import 7The ratio of difference in height be (1.1-1.2): 1; In described the first feed entrance 1, being connected with the first charging dividesCloth device 11; In described the second feed entrance 2, be connected with the second feed distributor 21; Described the first chargingBetween entrance 1 and described the second feed entrance 2, be provided with at least one in sieve plate, rotating disk and filler.In this preferred embodiment, extraction equipment of the present invention is particularly suitable for carrying out to comprising independent and relatively closeThe first feedstock oil that degree reduces successively and the described mink cell focus of the second feedstock oil extract; Wherein saidOne feedstock oil is 1-1.2g/mL the relative density of 20 DEG C, relatively close at 20 DEG C of described the second feedstock oilDegree is 0.9340-0.9995g/mL.
Wherein, as the particularly preferred a kind of embodiment of the present invention, described at least two feed entrance bagsDraw together the first feed entrance 1 and the second feed entrance 2; Described the first feed entrance 1 and described extractantDifference in height between import 7 is with respect between described the second feed entrance 2 and described extractant import 7The ratio of difference in height be (1.08-1.15): 1; In described the first feed entrance 1, be connected with the first chargingDistributor 11; In described the second feed entrance 2, be connected with the second feed distributor 21; Described first entersBetween material entrance 1 and described the second feed entrance 2, be provided with at least one in sieve plate, rotating disk and filler.In this preferred embodiment, extraction equipment of the present invention is particularly suitable for carrying out to comprising independent and relatively closeThe second feedstock oil that degree reduces successively and the described mink cell focus of the 3rd feedstock oil extract; Wherein saidTwo feedstock oils are 0.9340-0.9995g/mL the relative density of 20 DEG C, and described the 3rd feedstock oil is at 20 DEG CRelative density be 0.9-0.9335g/mL.
Wherein, as the particularly preferred a kind of embodiment of the present invention, described at least two feed entrances alsoComprise the 3rd feed entrance 3; Height between described the first feed entrance 1 and described extractant import 7The poor ratio with respect to the difference in height between described the second feed entrance 2 and described extractant import 7 of degreeFor (1.05-1.3): 1; Height between described the second feed entrance 2 and described extractant import 7Difference with respect to the ratio of the difference in height between described the 3rd feed entrance 3 and described extractant import 7 is(1.05-1.3): 1; In described the first feed entrance 1, be connected with the first feed distributor 11; DescribedIn two feed entrances 2, be connected with the second feed distributor 21; In described the 3rd feed entrance 3, be connected withThree feed distributors 31; Between described the first feed entrance 1 and described the second feed entrance 2 and described inBetween the second feed entrance 2 and described the 3rd feed entrance 3, be provided with in sieve plate, rotating disk and filler extremelyFew a kind of. In this preferred embodiment, extraction equipment of the present invention is particularly suitable for carrying out comprising independenceAnd the described mink cell focus of the first feedstock oil that relative density reduces successively, the second feedstock oil and the 3rd feedstock oilExtract; Wherein said the first feedstock oil is 1-1.2g/mL the relative density of 20 DEG C, described secondFeedstock oil is 0.9340-0.9995g/mL the relative density of 20 DEG C, and described the 3rd feedstock oil is at 20 DEG CRelative density is 0.9-0.9335g/mL.
Wherein, preferably, extractant import 7 is also connected with the extractant being placed in extraction tower 6 and dividesCloth device 71.
The present invention also provides a kind of method of processing mink cell focus, and described mink cell focus comprises independent and relatively closeTwo kinds of feedstock oils that degree reduces successively, the method comprises the bottom that extractant is passed into extraction equipment, willDescribed mink cell focus passes into the middle and upper part of extraction equipment, makes described mink cell focus and up described extractant contraryStream contact extracts; This extraction equipment comprises extraction tower 6 and is successively set on from top to bottom described extractionGet at least one extract outlet 4, at least one extractant import 7 and at least one raffinate on towerLiquid outlet 8; Between described extract outlet 4 and described extractant import 7, be provided with at least twoIndividual feed entrance, described at least two feed entrances comprise the first feed entrance 1 and the 3rd feed entrance 2;And described in being greater than, the difference in height between described the first feed entrance 1 and described extractant import 7 is fed intoDifference in height between mouth 2 and described extractant import 7; Wherein, described the first feed entrance 1 is introducedThe relative density of the feedstock oil introduced higher than described the second feed entrance 2 of the relative density of feedstock oil.
Wherein, preferably, described the first feed entrance 1 is introduced the first feedstock oil, described the first feedstock oilBe 1-1.2g/mL the relative densities of 20 DEG C, described the second feed entrance 2 is introduced the 3rd feedstock oil, instituteStating the 3rd feedstock oil is 0.9-0.9335g/mL the relative density of 20 DEG C. Wherein, pass into described extraction towerThe first feedstock oil of 6 and the volume ratio of the 3rd feedstock oil can change in a big way, for example, be 1:(0.1-5). Wherein, the difference in height between described the first feed entrance 1 and described extractant import 7Be greater than the difference in height between described the 3rd feed entrance 2 and described extractant import 7, for example instituteState difference in height between the first feed entrance 1 and described extractant import 7 with respect to described feed entrance2 and described extractant import 7 between the ratio of difference in height can be (1.03-1.5): 1, be preferably(1.05-1.3)：1。
Wherein, preferably, within the unit interval, pass into first feedstock oil and the 3rd of described extraction tower 6The volume ratio of feedstock oil is 1:(0.1-2).
Wherein, the extraction temperature in described extraction tower 6 can be 40-290 DEG C, is preferably 60-270 DEG C;More preferably, the column bottom temperature of described extraction tower 6 is 50-220 DEG C, and tower top temperature is 60-230 DEG C. InstituteState column bottom temperature lower than described tower top temperature.
Wherein, pass into volume and described the first feedstock oil and described of the extractant of described extraction tower 6The ratio of three raw material BVOs can change in a big way, for example, can be (0.5-20): 1,Be preferably (1-15): 1; More preferably (2-10): 1. Pass into the extractant of described extraction tower 6The ratio of volume and described the first feedstock oil and described the 3rd raw material BVO can be called ratio of solvent.The extractant that passes into described extraction tower 6 can partly or entirely pass into through extractant import 7.
Wherein, the extractant that passes into described extraction tower 6 can contain the hydrocarbon with 2-8 carbon atom.For example, described extractant include but not limited to ethane, propane, propylene, butane, pentane, hexane,At least one in heptane and octane. Preferred described extractant comprise alkane, the C4 of C4 alkene,At least one in the alkane of C5, the alkene of C5, the alkane of C6 and the alkene of C6.
Wherein, the pressure in extraction tower 6 can be 1-7MPa, is preferably 2-6MPa.
Wherein, particularly preferred a kind of embodiment according to the present invention, described the first feedstock oil is at 20 DEG CRelative density be 1-1.2g/mL, the relative density of described the 3rd feedstock oil at 20 DEG C is0.9-0.9335g/mL; Within the unit interval, pass into the first feedstock oil of described extraction tower 6 and the 3rd formerExpect that oily volume ratio is 1:0.1-2; Between described the first feed entrance 1 and described extractant import 7Difference in height with respect to the difference in height between described the second feed entrance 2 and described extractant import 7Ratio is (1.05-1.3): 1; Pass into the volume of extractant of described extraction tower 6 and described first formerThe ratio of material oil and described the 3rd raw material BVO is (3-7): 1; The alkane of described extractant C4In alkene, the alkane of C6 and the alkene of C6 of the alkene of hydrocarbon, C4, the alkane of C5, C5 at leastOne, as being the isopentane that contains 85-96%, the butane of 2-10 volume %.
Wherein, according to the present invention another preferred embodiment, described mink cell focus also comprises independentlyThe second feedstock oil, and described the first feedstock oil, described the second feedstock oil are relative with described the 3rd feedstock oilDensity reduces successively; Described at least two feed entrances also comprise the 3rd feed entrance 3, and described first entersMaterial entrance 1, described the second feed entrance 2 and described the 3rd feed entrance 3 and described extractant importDifference in height between 7 reduces successively; Wherein, described the first feedstock oil is passed into described the first feed entrance1, described the second feedstock oil is passed into described the second feed entrance 2, described in described the 3rd feedstock oil is passed intoThe 3rd feedstock oil entrance 3.
Wherein, the relative density of described the first feedstock oil, described the second feedstock oil and described the 3rd feedstock oilReduce successively, preferably, described the first feedstock oil is 1-1.2g/mL the relative density of 20 DEG C,Described the second feedstock oil is 0.9340-0.9995g/mL the relative density of 20 DEG C, described the 3rd feedstock oilBe 0.9-0.9335g/mL the relative densities of 20 DEG C; Within the unit interval, pass into described extraction tower 6The volume ratio of the first feedstock oil and the second feedstock oil is 1:(0.1-15); Pass into of described extraction tower 6The volume ratio of one feedstock oil and the 3rd feedstock oil is 1:(0.1-5); Described the first feed entrance 1 with described inDifference in height between extractant import 7 is entered with described extractant with respect to described the second feed entrance 2The ratio of the difference in height between mouth 7 is (1.05-1.3): 1; Described the second feed entrance 2 and described extractionGet difference in height between solvent inlet 7 with respect to described the 3rd feed entrance 3 and described extractant importThe ratio of the difference in height between 7 is (1.05-1.3): 1.
Wherein, more preferably, within the unit interval, pass into first feedstock oil and of described extraction tower 6The volume ratio of two feedstock oils is 1:(1-10), pass into the first feedstock oil of described extraction tower 6 and the 3rd formerExpect that oily volume ratio is 1:(0.5-3).
Wherein, the temperature of described extraction tower can change according to solvent used, for example, and described extractionGetting tower 6 extraction temperature can be 40-290 DEG C, is preferably 60-270 DEG C, particularly preferably, and described extractionThe column bottom temperature of tower 6 is 50-185 DEG C, and tower top temperature is 60-195 DEG C, and this particularly preferred temperature is applicable toWith the alkane of the alkene of the alkane of the alkene of the alkane that contains C3, C3, C4, C4, C5 and C5At least one in alkene, as being the normal butane of 5-10 volume %, the iso-butane of 40-60 volume %,The extraction that the isobutene of the n-butene of 10-15 volume % and 20-30 volume % carries out. Described column bottom temperatureLower than described tower top temperature.
Wherein, the pressure of described extraction tower can change according to solvent used, for example, and described extractionThe pressure of getting tower 6 can be 1-7MPa, preferably 2-6MPa.
Wherein, pass into volume and described first feedstock oil, described of the extractant of described extraction tower 6The ratio of two feedstock oils and described the 3rd raw material BVO can change in a big way, for example canThink (0.5-20): 1, be preferably (1-15): 1; More preferably (2-10): 1.
Wherein, the extractant that passes into described extraction tower 6 can contain the hydrocarbon with 2-8 carbon atom;For example, described extractant include but not limited to ethane, propane, propylene, butane, pentane, hexane,At least one in heptane and octane. Preferred described extractant comprise alkane, the C3 of C3 alkene,At least one in the alkane of C4, the alkene of C4, the alkane of C5 and the alkene of C5, as being 5-10The normal butane of volume %, the iso-butane of 40-60 volume %, the n-butene of 10-15 volume % and 20-30 bodyThe isobutene of long-pending %.
Wherein, a kind of particularly preferred embodiment according to the present invention, described the first feedstock oil, described theThe relative density of two feedstock oils and described the 3rd feedstock oil reduces successively, preferably, described first formerThe material oil relative density at 20 DEG C is 1-1.2g/mL, relatively close at 20 DEG C of described the second feedstock oilDegree is 0.9340-0.9995g/mL, and the relative density of described the 3rd feedstock oil at 20 DEG C is0.9-0.9335g/mL; Within the unit interval, pass into the first feedstock oil of described extraction tower 6 and second formerExpect that oily volume ratio is 1:1-10; Pass into the first feedstock oil of described extraction tower 6 and the 3rd feedstock oilVolume ratio is 1:0.5-3; Height between described the first feed entrance 1 and described extractant import 7Difference with respect to the ratio of the difference in height between described the second feed entrance 2 and described extractant import 7 is(1.05-1.3): 1; Difference in height between described the second feed entrance 2 and described extractant import 7Ratio with respect to the difference in height between described the 3rd feed entrance 3 and described extractant import 7 is(1.05-1.3): 1; Pass into the volume of extractant of described extraction tower 6 and described the first feedstock oil,The ratio of described the second feedstock oil and described the 3rd raw material BVO is (1-15): 1; Described extractionThe normal butane that solvent contains 5-10 volume %, the iso-butane of 40-60 volume %, the positive fourth of 10-15 volume %The isobutene of alkene and 20-30 volume %.
Wherein, according to method of the present invention, meet described the first raw material that above-mentioned relative density requiresOil can be Canadian oil sands bitumen, bitumen, the decompression slag that 20 DEG C of relative densities are 1-1.2g/mLAt least one in oil and reduced crude; Described the second feedstock oil comprises that 20 DEG C of relative densities areAt least one in decompression residuum, reduced crude and the visbroken resids of 0.9340-0.9995g/mL;Described the 3rd feedstock oil comprise decompression residuum that 20 DEG C of relative densities are 0.9-0.9335g/mL, reduced crude,At least one in fixed bed hydrogenation residual oil and wax tailings. Conventional residual oil can comprise reduced crude and subtractPress residual oil; Reduced crude refers to that the boiling range that crude oil obtains after normal pressure fractionation is to be greater than the cut of 350 DEG C;Decompression residuum refers to that the boiling range that reduced crude obtains after vacuum fractionation is to be greater than the cut of 500 DEG C. AddHydrogen residual oil refers to that boiling range that hydrogenation products that residual oil obtains through fixed bed hydrogenation obtains after fractionation is for being greater thanThe cut of 350 DEG C.
Wherein, can improve by the heater in described extraction tower 6 temperature of tower top, to increase extractionSelective.
Wherein, the material of deriving from raffinate outlet 8, contain de-oiled asphalt, this material can be as burntChange in raw material, slurry bubble bed hydrogenating materials, gasified raw material, hard grades of bitumen modifier and boiler oil at leastA kind of.
Further describe by the following examples the present invention.
Embodiment 1
The present embodiment illustrates comprising described the first feedstock oil, described the second feedstock oil and the described the 3rdThe method that the mink cell focus of feedstock oil is processed. Wherein the source of the first feedstock oil is raw material in Saudi ArabiaDecompression residuum, the source of the second feedstock oil is the decompression residuum of raw material in winning, the 3rd feedstock oilSource is the hydrogenated residue of raw material in triumph, analyzes their character, knot according to country or professional standardFruit is as shown in table 1.
Table 1
| Analysis project | The first feedstock oil | The second feedstock oil | The 3rd feedstock oil |
| Relative density (2O DEG C), g/cm3 | 1.052 | 0.9665 | 0.9163 |
| Viscosity (10O DEG C), mm2/s | 3856 | 386 | 82.46 |
| Carbon residue, % by weight | 23.3 | 12.7 | 7.3 |
| Saturated part, % by weight | 8.8 | 23.7 | 37.6 |
| Fragrance part, % by weight | 51.9 | 41.9 | 38.3 |
| Colloid, % by weight | 29.1 | 27.5 | 23.5 |
| Asphalitine, % by weight | 10.2 | 6.9 | 0.6 |
| C, % by weight | 84.03 | 86.42 | 86.9 |
| H, % by weight | 10.04 | 10.97 | 12.5 |
| H/C mol ratio | 1.43 | 1.52 | 1.72 |
With reference to figure 1, extraction equipment is set, this extraction equipment comprises extraction tower 6 and from top to bottom successivelyArrange and the extract that is communicated with described extraction tower exports 4, the first feed entrance 1, the second feed entrance 2,The 3rd feed entrance 3, extractant import 7 and raffinate outlet 8, the first feed entrances 1 and extractionDifference in height between solvent inlet 7 is with respect to the height between the second feed entrance 2 and extractant import 7The poor ratio of degree is 1.15:1; Difference in height phase between the second feed entrance 2 and extractant import 7Be 1.15:1 for the ratio of the difference in height between the 3rd feed entrance 3 and extractant import 7. TheOne feed entrance 1 is connected with the first feed distributor 11 being placed in extraction tower; The second feed entrance 2Be connected with the first feed distributor 21 being placed in extraction tower; The 3rd feed entrance 3 be placed in extraction towerThe first interior feed distributor 31 connects; In extraction tower, the first feed entrance 1 and second is fed intoBetween mouth 2, be provided with the first filler 111; Between the second feed entrance 2 and the 3rd feed entrance 3, arrangeThere is the second filler 211; Between the 3rd feed entrance 3 and extractant import 7, be provided with the 3rd filler 311;Filler as above is structured packing.
With reference to figure 1, the first feedstock oil is passed into the first feed entrance 1, described the second feedstock oil is passed intoDescribed the second feed entrance 2, passes into the 3rd feedstock oil entrance 3 by described the 3rd feedstock oil; Extraction tower 6Column bottom temperature be 90 DEG C; The tower top temperature of extraction tower 6 is 110 DEG C. Extractant is passed into extraction moltenAgent import 7; The normal butane that extractant contains 7.1 volume %, the iso-butane of 50.7 volume %, 12.6 bodiesThe n-butene of long-pending %, the isobutene of 26.6 volume %. The pressure of extraction tower is 4.0MPa, and total solvent ratio is5:1, wherein total solvent ratio referred within the unit interval, pass into extraction tower 6 solvent volume with respect toThe ratio of the first feedstock oil, the second feedstock oil and the 3rd raw material BVO; Within the unit interval, logicalThe ratio that enters the volume of extraction tower the first feedstock oil, the second feedstock oil and the 3rd feedstock oil is 1:7:2.Derive extract from extract outlet 4, derive raffinate from raffinate outlet 8.
Comparative example 1
Use the extraction equipment described in embodiment 1 to extract, different, sealing first is fed intoMouthful 1 and second feed entrance 2, by the first feedstock oil, the second feedstock oil and the 3rd feedstock oil according to 1:7:2 ratio imports extraction tower 6 through the 3rd feed entrance 3 after mixing.
Comparative example 2
Use the extraction equipment described in embodiment 1 to extract, different, sealing second and the 3rdEntrance, after the first feedstock oil, the second feedstock oil and the 3rd feedstock oil are mixed according to the ratio of 1:7:2,Import extraction tower 6 through the first feed entrance 1.
Test implementation example 1
According to the method in national standard, measure embodiment 1 and comparative example 1,2 and be extracted thing removalThe character of the product after extractant, result is as shown in table 2.
Table 2
| Analysis project | Embodiment 1 | Comparative example 1 | Comparative example 2 |
| Yield | 82.6 | 77.8 | 78.9 |
| Viscosity (100 DEG C), mm2/s | 51.1 | 52.4 | 52.1 |
| Carbon residue, % by weight | 6.2 | 7.1 | 6.9 |
| Ni，μg/g | 2.6 | 2.9 | 2.9 |
| V，μg/g | 14.5 | 15.6 | 15.7 |
Visible according to the data of table 2, extraction equipment provided by the invention and method can improve extraction significantlyGet the efficiency of mink cell focus.
Embodiment 2
The present embodiment illustrates the mink cell focus to comprising described the first feedstock oil and described the 3rd feedstock oilThe method of processing. Wherein the source of the first feedstock oil is overweight residual oil, and the source of the 3rd feedstock oil isHydrogenated residue, according to country and their character of professional standard analysis, result is as shown in table 3.
Table 3
| Analysis project | The first feedstock oil | The 3rd feedstock oil |
| Relative density (2O DEG C), g/cm3 | 1.0330 | 0.9163 |
| Viscosity (10O DEG C), mm2/s | 4024 | 82.46 |
| Carbon residue, % by weight | 23.5 | 7.3 |
| Saturated part, % by weight | 8.3 | 37.6 |
| Fragrance part, % by weight | 52.4 | 38.3 |
| Colloid, % by weight | 25.8 | 23.5 |
| Drop table matter, % by weight | 13.5 | 0.6 |
| C, % by weight | 84.0 | 86.9 |
| H, % by weight | 10.1 | 12.5 |
| H/C mol ratio | 1.42 | 1.72 |
With reference to figure 2, extraction equipment is set, this extraction equipment comprises extraction tower 6 and from top to bottom successivelyArrange and the extract that is communicated with described extraction tower exports 4, the first feed entrance 1, the second feed entrance 2,Between extractant import 7 and raffinate outlet 8, the first feed entrances 1 and extractant import 7Difference in height is 1.15 with respect to the ratio of the difference in height between the second feed entrance 2 and extractant import 7:1. The first feed entrance 1 is connected with the first feed distributor 11 being placed in extraction tower; Second is fed intoMouth 2 is connected with the first feed distributor 21 being placed in extraction tower; In extraction tower, first is fed intoBetween mouth 1 and the second feed entrance 2, be provided with the first filler 111; The second feed entrance 2 is molten with extractionBetween agent import 7, be provided with the second filler 211; Filler as above is structured packing.
With reference to figure 2, the first feedstock oil is passed into the first feed entrance 1, described the 3rd feedstock oil is passed intoDescribed the second feed entrance 2, the column bottom temperature of extraction 6 is 170 DEG C; The tower top temperature of extraction tower 6 is180 DEG C. Extractant is passed into extractant import 7; Isopentane that extractant contains 92 volume %,The normal butane of 5.5 volume %. Pressure in extraction tower is 4.0MPa, and total solvent is than being 6:1, Qi ZhongzongRatio of solvent refers within the unit interval, the volume of solvent that passes into extraction tower 6 with respect to the first feedstock oil andThe ratio of the 3rd raw material BVO; Within the unit interval, pass into extraction tower the first feedstock oil and the 3rdThe ratio of the volume of feedstock oil is 1:1. Derive extract from extract outlet 4, from raffinate outlet 8Derive raffinate.
Comparative example 3
Use the extraction equipment described in embodiment 6 to extract, different, sealing first is fed intoMouthful 1, after the first feedstock oil and the 3rd feedstock oil are mixed according to the ratio of 1:1, be fed into through secondMouth 2 imports extraction towers 6.
Comparative example 4
Use the extraction equipment described in embodiment 6 to extract, different, sealing second is fed intoMouthfuls two, after the first feedstock oil and the 3rd feedstock oil are mixed according to the ratio of 1:1, through the first chargingEntrance 1 imports extraction tower 6.
Test implementation example 2
According to the analytical method in country and professional standard, measure embodiment 2 and comparative example 3,4 and obtainExtract is removed the character of the product after extractant, and result is as shown in table 4.
Table 4
| Analysis project | Embodiment 2 | Comparative example 3 | Comparative example 4 |
| Yield | 73.32 | 68.34 | 70.10 |
| Viscosity (10O DEG C), mm2/s | 89.3 | 94.6 | 91.6 |
| Carbon residue, % by weight | 7.34 | 9.69 | 8.37 |
| Ni，μg/g | 4.3 | 4.9 | 4.6 |
| V，μg/g | 13.5 | 16.2 | 15.4 |
Visible according to the data of table 4, extraction equipment provided by the invention and method can improve extraction significantlyGet the efficiency of mink cell focus.
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 (24)
1. an extraction equipment, this extraction equipment comprises extraction tower (6) and sets gradually from top to bottomAt least one extract outlet (4), at least one extractant import (7) on described extraction towerWith at least one raffinate outlet (8); It is characterized in that: in the described extraction of described extraction tower (6)Between thing outlet (4) and described extractant import (7), be provided with at least two feed entrances, instituteState at least two feed entrances and comprise the first feed entrance (1) and the second feed entrance (2); And described inDifference in height between the first feed entrance (1) and described extractant import (7) is greater than described second and entersDifference in height between material entrance (2) and described extractant import (7).
2. extraction equipment according to claim 1, is characterized in that: described the first feed entrance(1) difference in height and between described extractant import (7) is with respect to described the second feed entrance (2)And the ratio of the difference in height between described extractant import (7) is (1.05-1.3): 1.
3. extraction equipment according to claim 1, is characterized in that: described at least two chargingsEntrance also comprises the 3rd feed entrance (3); And described the second feed entrance (2) and described extractantDifference in height between import (7) is greater than described the 3rd feed entrance (3) and described extractant import (7)Between difference in height.
4. extraction equipment according to claim 3, is characterized in that: described the first feed entrance(1) difference in height and between described extractant import (7) is with respect to described the second feed entrance (2)And the ratio of the difference in height between described extractant import (7) is (1.05-1.3): 1; Described secondDifference in height between feed entrance (2) and described extractant import (7) is with respect to described the 3rd chargingThe ratio of the difference in height between entrance (3) and described extractant import (7) is (1.05-1.3): 1.
5. according to the extraction equipment described in any one in claim 1-4, it is characterized in that: described inFeed entrance is connected with or is not connected with the feed distributor being placed in extraction tower independently.
6. according to the extraction equipment described in any one in claim 1-4, it is characterized in that: described inBetween feed entrance and described extractant import (7), be provided with the sieve plate, the rotating disk that are placed in extraction towerWith at least one in filler.
7. extraction equipment according to claim 6, is characterized in that: the institute that at least one pair of is adjacentState and between feed entrance, be provided with at least one in sieve plate, rotating disk and filler.
8. extraction equipment according to claim 1, is characterized in that: described at least two chargingsEntrance comprises the first feed entrance (1) and the second feed entrance (2); Described the first feed entrance (1)And the difference in height between described extractant import (7) is with respect to described the second feed entrance (2) and instituteThe ratio of stating the difference in height between extractant import (7) is (1.2-1.3): 1; Described the first chargingOn entrance (1), be connected with the first feed distributor (11); Described the second feed entrance (2) is upper to be connectedThere is the second feed distributor (21); Described the first feed entrance (1) and described the second feed entrance (2)Between be provided with at least one in sieve plate, rotating disk and filler.
9. extraction equipment according to claim 1, is characterized in that: described at least two chargingsEntrance comprises the first feed entrance (1) and the second feed entrance (2); Described the first feed entrance (1)And the difference in height between described extractant import (7) is with respect to described the second feed entrance (2) and instituteThe ratio of stating the difference in height between extractant import (7) is (1.1-1.2): 1; Described the first chargingOn entrance (1), be connected with the first feed distributor (11); Described the second feed entrance (2) is upper to be connectedThere is the second feed distributor (21); Described the first feed entrance (1) and described the second feed entrance (2)Between be provided with at least one in sieve plate, rotating disk and filler.
10. extraction equipment according to claim 1, is characterized in that: described at least two chargingsEntrance comprises the first feed entrance (1) and the second feed entrance (2); Described the first feed entrance (1)And the difference in height between described extractant import (7) is with respect to described the second feed entrance (2) and instituteThe ratio of stating the difference in height between extractant import (7) is (1.08-1.15): 1; Described first entersOn material entrance (1), be connected with the first feed distributor (11); In described the second feed entrance (2), connectBe connected to the second feed distributor (21); Described the first feed entrance (1) and described the second feed entrance (2)Between be provided with at least one in sieve plate, rotating disk and filler.
11. extraction equipments according to claim 1, is characterized in that: described at least two chargingsEntrance also comprises the 3rd feed entrance (3); Described the first feed entrance (1) is entered with described extractantDifference in height between mouthful (7) with respect to described the second feed entrance and described extractant import (7) itBetween the ratio of difference in height be (1.05-1.3): 1; Described the second feed entrance (2) is molten with described extractionDifference in height between agent import (7) is entered with respect to described the 3rd feed entrance (3) and described extractantThe ratio of the difference in height between mouth (7) is (1.05-1.3): 1; In described the first feed entrance (1)Be connected with the first feed distributor (11); In described the second feed entrance (2), being connected with the second charging dividesCloth device (21); In described the 3rd feed entrance (3), be connected with the 3rd feed distributor (31); DescribedBetween the first feed entrance (1) and described the second feed entrance (2) and described the second feed entrance (2)And be provided with at least one in sieve plate, rotating disk and filler between described the 3rd feed entrance (3).
Process the method for mink cell focus for 12. 1 kinds, described mink cell focus comprises that independence and relative density reduce successivelyTwo kinds of feedstock oils, the method comprises the middle and lower part that extractant is passed into extraction equipment, by described heavyOil passes into the middle and upper part of extraction equipment, and described mink cell focus and up described extractant counter current contacting are enteredRow extraction; Described extraction equipment comprises extraction tower (6) and is successively set on from top to bottom described extractionAt least one extract outlet (4) on tower (6), at least one extractant import (7) and at leastA raffinate outlet (8); It is characterized in that: molten in described extract outlet (4) and described extractionBetween agent import (7), be provided with at least two feed entrances; Described at least two feed entrances compriseThe first feed entrance (1) and the second feed entrance (2), and described the first feed entrance (1) with described inIt is molten with described extraction that difference in height between extractant import (7) is greater than described the second feed entrance (2)Difference in height between agent import (7); Wherein, the feedstock oil that described the first feed entrance (1) is introducedThe relative density of the feedstock oil that relative density is introduced higher than described the second feed entrance (2).
13. methods according to claim 12, is characterized in that: described the first feed entrance (1)Introduce the first feedstock oil, described the first feedstock oil is 1-1.2g/mL the relative density of 20 DEG C, describedTwo feed entrances (2) are introduced the 3rd feedstock oil, and described the 3rd feedstock oil the relative density of 20 DEG C is0.9-0.9335g/mL; Within the unit interval, pass into first feedstock oil and the 3rd of described extraction tower (6)The volume ratio of feedstock oil is 1:(0.1-5); Described the first feed entrance (1) is entered with described extractantDifference in height between mouth (7) is with respect to described the second feed entrance (2) and described extractant import (7)Between the ratio of difference in height be (1.05-1.3): 1.
14. methods according to claim 13, is characterized in that: within the unit interval, pass intoThe first feedstock oil of described extraction tower (6) and the volume ratio of the 3rd feedstock oil are 1:(0.1-2).
15. methods according to claim 13, is characterized in that: the tower of described extraction tower (6)End temperature is 50-220 DEG C, and tower top temperature is 60-230 DEG C; Pressure in described extraction tower (6) is 2-6MPa.
16. methods according to claim 13, is characterized in that: pass into described extraction tower (6)The volume of extractant and the ratio of described the first feedstock oil and described the 3rd raw material BVO be(1-15)：1。
17. according to the method described in any one in claim 13-16, it is characterized in that: described extractionGet alkane, the C5 of alkene, the C5 of alkane that solvent contains C4, C4 alkene, C6 alkane andAt least one in the alkene of C6.
18. methods according to claim 12, is characterized in that: described mink cell focus also comprises solelyThe second vertical feedstock oil, and described the first feedstock oil, described the second feedstock oil and described the 3rd feedstock oilRelative density reduces successively; Described at least two feed entrances also comprise the 3rd feed entrance (3), described inThe first feed entrance (1), described the second feed entrance (2) and described the 3rd feed entrance (3) and instituteThe difference in height of stating between extractant import (7) reduces successively; Wherein, described the first feedstock oil is logicalEnter described the first feed entrance (1), described the second feedstock oil passed into described the second feed entrance (2),Described the 3rd feedstock oil is passed into described the 3rd feedstock oil entrance (3).
19. methods according to claim 18, is characterized in that: described the first feedstock oil is at 20 DEG CRelative density be 1-1.2g/mL, described the second feedstock oil the relative density of 20 DEG C is0.934-0.9995g/mL, described the 3rd feedstock oil is 0.9-0.9335g/mL the relative density of 20 DEG C;Within the unit interval, pass into the volume ratio of the first feedstock oil and second feedstock oil of described extraction tower (6)For 1:(0.1-15); Pass into the volume ratio of the first feedstock oil and the 3rd feedstock oil of described extraction tower (6)For 1:(0.1-5); Height between described the first feed entrance (1) and described extractant import (7)Degree is poor with respect to the difference in height between described the second feed entrance (2) and described extractant import (7)Ratio be (1.05-1.3): 1; Described the second feed entrance (2) and described extractant import (7)Between difference in height with respect between described the 3rd feed entrance (3) and described extractant import (7)The ratio of difference in height be (1.05-1.3): 1.
20. method according to claim 19, is characterized in that: within the unit interval, pass intoThe first feedstock oil of described extraction tower (6) and the volume ratio of the second feedstock oil are 1:(1-10), pass into instituteState the first feedstock oil of extraction tower (6) and the volume ratio of the 3rd feedstock oil is 1:(0.5-3).
21. methods according to claim 19, is characterized in that: the tower of described extraction tower (6)End temperature is 50-185 DEG C, and tower top temperature is 60-195 DEG C; The pressure of extraction tower (6) is 2-6MPa.
22. methods according to claim 19, is characterized in that: pass into described extraction tower (6)The volume of extractant and described the first feedstock oil, described the second feedstock oil and described the 3rd feedstock oilThe ratio of cumulative volume is (1-15): 1.
23. according to the method described in any one in claim 19-22, it is characterized in that: described in warpThe alkane of the alkane that the extractant that extractant import (7) passes into contains C3, the alkene of C3, C4,At least one in the alkene of the alkene of C4, the alkane of C5 and C5.
24. method according to claim 19, is characterized in that: described the first feedstock oil comprisesThe relative density of 20 DEG C is Canadian oil sands bitumen, bitumen, the decompression residuum and normal of 1-1.2g/mLPress at least one in residual oil; Described the second feedstock oil comprises that the relative density of 20 DEG C is 0.9340-0.9995At least one in decompression residuum, reduced crude and the visbroken resids of g/mL; Described the 3rd raw materialOil comprises that decompression residuum, reduced crude, fixed bed that the relative density of 20 DEG C is 0.9-0.9335g/mL addAt least one in hydrogen residual oil and wax tailings.
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| CN111088060A (en) * | 2018-10-24 | 2020-05-01 | 中国石油化工股份有限公司 | System and method for viscosity reduction |
| CN111088063A (en) * | 2018-10-24 | 2020-05-01 | 中国石油化工股份有限公司 | System and method for viscosity reduction |
| CN111088061A (en) * | 2018-10-24 | 2020-05-01 | 中国石油化工股份有限公司 | System and method for viscosity reduction |
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| CN111088063B (en) * | 2018-10-24 | 2021-08-03 | 中国石油化工股份有限公司 | System and method for viscosity reduction |
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