CN1083513A - A kind of method of separating petroleum heavy oil - Google Patents
A kind of method of separating petroleum heavy oil Download PDFInfo
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- CN1083513A CN1083513A CN 93117577 CN93117577A CN1083513A CN 1083513 A CN1083513 A CN 1083513A CN 93117577 CN93117577 CN 93117577 CN 93117577 A CN93117577 A CN 93117577A CN 1083513 A CN1083513 A CN 1083513A
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Abstract
The present invention utilizes the supercritical fluid extraction principle, has developed a kind ofly to comprise C with lighter hydrocarbons
3, nC
4, iC
4, nC
5Or their mixture is the supercritical fluid extraction fractionating method and the tripping device of solvent.Under tripping device extraction and fractionation post steady temperature gradient, adopt linear boosting mode, can be with petroleum heavy oil, particularly petroleum residual oil roughly cuts into tens or even more a plurality of narrow fraction by the size of molecular weight.Have good separating effect, process is simple, near producing actual characteristics; To producing the actual directive function that has.
Description
This bright method that relates to a kind of separating hydrocarbons mixture is especially utilized the method for supercritical solvent extraction separating mixture.
Petroleum heavy oil has the boiling point height as other heavy products of producing in oil long residuum, vacuum residuum and the refining process etc., and poor heat stability is formed very complicated characteristics.Estimate it, primary problem is must be earlier it to be carried out to a certain degree separation.Up to now, mostly be to adopt the flushed in liquid phase chromatography as main separation means, be separated into saturated part, fragrance part, colloid and four of bituminous matters or more a plurality of by group composition,, respectively the chemical constitution and the average structure of these components studied then as six to ten components.This method is from instructing the angle of development mink cell focus utilization and processing technology, the wretched insufficiency part is still arranged, mainly show: (1) chromatography separating method is loaded down with trivial details, and the gained sample size seldom, is difficult to therefrom obtain to satisfy necessary various basic datas and information on the engineering; (2) chromatographic separation principle and production process are too wide in the gap, and it is actual that the achievement in research that obtains thus is not easy to use production.
US3597464(1971), Zosel discloses a kind of fractionated method of supercritical fluid extraction of utilizing, utilize overcritical ethene or ethane to be solvent, adopt the constant separator column temperature difference and stepped start-stop system boosting mode, with the trialkylaluminium mixture of different chain length, be separated into the comparatively single organo-aluminium compound of chain length.US3969169(1976) Zosel discloses with ethane and has made solvent, with the method and apparatus of above-mentioned US3597464 with C
16To C
26The alpha-olefin mixture separation become every kind of compound purity can reach the fraction of 95-99%.Zosel, Angew.Chem.Int.Ed.Engl., 1978; 17,702 to have delivered with overcritical ethene be solvent, utilizes aforesaid method that haddock liver oil successfully is separated into 50 fractions by the size of molecular weight and degree of unsaturation.
R.P.Wanzinski, etal., preprints-ACS, Div.Fuel Chem., 1.243 1985; Delivered similar tripping device with above-mentioned Zosel, with overcritical hexanaphthene is solvent, adopts constant pressure and substep to reduce the separator column head temperature, promptly reduces the mode of the separator column temperature difference, with 6 close-cut fractions of the separating of oil one-tenth of coal liquefaction residue, so that measure its thermodynamic property better.
In the aforesaid method, in the technology of Wanzinski, because the stabilization ratio pressure-stabilisation of system temperature is much more difficult, so separate by this method, its reliability and poor repeatability, and in the technology of Wanzinski and Zosel, the temperature difference of supercritical fluid extraction fractional column is hollow separator (the Finger-shaped Hollow separator) realization that relies on the thermal backflow head (Hot Finger) of the well heater at separator column top and so-called picture " finger " shape or be called " finger " shape.This just makes the structure of equipment and makes comparatively complexity, and in the Zosel technology, supercutical fluid directly enters the separator column extraction section with pipeline.In the technology of Wanzinski, enter extraction section though pointed out supercutical fluid in the document by " sparger ", undeclared structure and principle.The method of Zosel is unsuitable for the separate evaluation of petroleum residual oil, because 1 Zosel uses ethene or ethane to make solvent, they are to petroleum heavy oil, and particularly the dissolving power of petroleum residual oil is too low, and extracted residues is too many, be difficult to realize that particularly petroleum residual oil carries out thoroughly evaluating to petroleum heavy oil; It is that separation condition is to separating petroleum heavy oil that 2 Zosel adopt constant temperature difference stepped start-stop system step-up method, the non-constant width of this boiling range scope of petroleum residual oil particularly, the system of forming very complicated and component continuous distribution, its " step by step " quantification of boosting is difficult to grasp, and pressure of every rising, the capital produces steadily carrying out of an interference separation process, thereby makes the repeatability of same laboratory separating resulting and the reproducibility of different experiments chamber separating resulting all be difficult to guarantee.
Also there are two problems in the method for Wanzinski: (1) he select for use cyclohexane to make solvent, and its critical temperature is 281 ℃.Separation temperature must be higher than critical temperature, can reach more than 300 ℃.Thermolysis can take place in petroleum heavy oil, particularly petroleum residual oil for a long time under this temperature action, should not be used to set up evaluation method.And the cyclohexane molecular weight is big, separation selectivity is poor, is difficult to satisfy the requirement of separation accuracy; (2) adopted constant pressure on technology, substep reduces the method for column top temperature.The shortcoming of this method is: the lifting of testing apparatus temperature and keep and stable want the lifting of specific pressure and stablize much more difficultly, this is difficult to guarantee the repeatability and the separating effect of testing can not satisfy the separate evaluation method of setting up petroleum heavy oil.
US4290880 adopts the fractional sedimentation method, sepn process is to realize by mixing tank three separators different with temperature condition, each separator can only obtain a product, therefore, adopt this process can only obtain three products, and every section separate not had " internal reflux " and produce, no fractionation, thereby separating effect has fractionation is poor.
Day disclosure special permission (A) clear 61-254693, set up an extraction tower than US4290880, be divided into two sections, top is enriching section, the bottom is a recovery zone, residual oil enters continuously from the extraction tower middle part, solvent enters from the extraction tower bottom, carries out counter-current extraction, and extraction tower top and bottom are respectively equipped with heat exchanger, keep head temperature to be higher than bottom temp, therefore, at enriching section the generation of backflow is arranged, its separating effect is better than the United States Patent (USP) technology, this process can obtain four products, and everywhere temperature in the process, pressure condition, logistics capacity and character are constant, its extraction tower top extract is a wide fraction, and its separation is to finish by three follow-up separators.
The objective of the invention is to set up a kind of separation principle close with production process can be under lower temperature with petroleum heavy oil, roughly cut into the method and the device of tens or more a plurality of needed close-cut fractions by the molecular weight size, for setting up petroleum heavy oil, particularly the evaluation method of petroleum residual oil provides a kind of effective separation means.
Purpose of the present invention realizes by following scheme:
Mink cell focus is sent in the extraction kettle (1) of supercritical liq extraction and fractionation post, with C
3, C
4, nC
5Or their mixture is a solvent, supercharging heats to being higher than its emergent pressure and critical temperature, make supercutical fluid enter extraction kettle 1 from " way flow " formula supercutical fluid sparger 3 of extraction kettle 1 bottom of supercritical fluid extraction fractional column bottom, fully contact with raw material, extract, form two-phase; The supercutical fluid that is dissolved with part material is flowed through in opposite directions and is raise to going up temperature down, and filling batch 5 with constant temp gradient, packing section is φ 2 * 2mm stainless steel θ ring, bed temperature is 100-250 ℃, make the dissolved raw material of part separate out downward inflow packing layer and form backflow, the pressure of extraction and fractionation post adopts linear boosting mode during separation, and pressure can be 3.5-20MPa, rate of rise 0.5-1.5MPa/hr realizes extraction and fractionation; The supercutical fluid that flows through filling batch is from column top spout flow through water cooler 7 and pressure regulator valve 9-1, after being decompressed to 0.2-2.0MPa, enter solvent product separator 14-1, electrically heated is to 100-200 ℃ of separation that realizes the two, product cuts into any fraction that needs by the molecular weight size, collects vacuum-drying by collector 16, solvent uses through refrigeration cycle, can replenish when solvent is not enough.
In the aforesaid method, the temperature of extraction and fractionation post has the constant temp gradient, and its extraction kettle temperature is higher than 10-50 ℃ of solvent critical temperature, and column top temperature is higher than at the bottom of the post temperature 10-80 ℃, and the flow rate of circulating solvent is 60-200ml/ branch (liquid).
The supercritical fluid extraction fractionation plant that separates petroleum heavy oil comprises: the raw material fresh feed pump, the solvent preheating oven, high-pressure solvent pump, the supercritical fluid extraction fractional column, the solvent product separator, the solvent cylinder, the supercutical fluid water cooler, solvent condenses water cooler and temperature, pressure calculate the machine Controlling System, the extraction and fractionation post is divided into extraction kettle and fractionation section two portions, be equipped with one in the extraction kettle bottom and can prevent that extracted residues from blowing back into " way flow " supercutical fluid sparger of solvent line, this sparger comprises a limit screw cap, a unsteady cone and a base; The heating unit that the extraction and fractionation post adopts is three sections electricity insulation heating, by microcomputer control, to realize the extraction and fractionation post uniform temperature gradient is arranged, and realizes that with micro-processor controlled stepper-motor drive needle-valve the linearity of extraction and fractionation post boosts.
The present invention compared with prior art has following advantage:
The present invention selects C for use
3, C
4(comprise iC
4), nC
5Or their mixture as solvent, be one of important feature that is different from prior art.Increase because the solvent ability of lighter hydrocarbons is the increases with carbonatoms, isolating selectivity then increases and variation with carbonatoms.If select C for use
2Or C
- 2Make solvent, even operation under high pressure, to petroleum heavy oil, particularly the sucrose extraction of petroleum residual oil is very low, has also just lost the original connotation of separate evaluation petroleum heavy oil.Make solvent if select the higher lighter hydrocarbons of carbonatoms (as cyclohexane etc.) for use, not only separation selectivity is poor, influence the practicality of result of study, also because its higher critical temperature, must cause sepn process to carry out under higher temperature (as being higher than 300 ℃), it is rotten to cause petroleum heavy oil to decompose.The mutual solubility of solute and solvent is to influence the vital factor of system phase behavior.Therefore, this also is one of key factor that influences separating effect.Under given solvent, the mutual solubility of the mink cell focus that solvent and boiling point are lower or molecular weight is less is bigger, and under the condition of fixing petroleum heavy oil, lighter hydrocarbons solvent and its mutual solubility that carbonatoms is many are also bigger.The mutual solubility of solvent and solute is too little, can cause sucrose extraction too low, and mutual solubility is too strong, causes separation selectivity to descend again, even can not realize normal centrifugation.For example, when selecting nC for use
5When making the separated from solvent heavy vacuum gas oil, just be difficult to obtain the ideal separating resulting, when being used to separate oil vacuum residuum, sucrose extraction height not only, isolating selectivity also can meet the demands.
Because the present invention has adopted the constant temperature difference, the separation condition that linearity is boosted, this just makes the repeatability of same laboratory separating resulting and the reproducibility of different experiments chamber separating resulting be guaranteed, and the constant temperature difference that Zosel adopts and stepped start-stop system boosting mode are to separating petroleum heavy oil, the non-constant width of this boiling range scope of petroleum residual oil particularly, the system of forming very complicated and component continuous distribution, its " step by step " quantification of boosting is difficult to grasp, and pressure of every rising, the capital produces steadily carrying out of an interference separation, thereby the Repeatability and Reproducibility that makes experiment is difficult to guarantee that .Wanzinski has adopted constant pressure, substep reduces the method for column top temperature, because the lifting of unit temp and keep the stable lifting of wanting specific pressure and stable difficult many, this is difficult to guarantee the repeatability and the separating effect of testing be difficult to satisfy the requirement of the separate evaluation method of setting up petroleum heavy oil.
The present invention does not have well heater and heat exchanger at the fractionation capital, and the temperature difference guarantees by segmentation electricity insulation heating, and system heat sources is mainly from the solvent preheating oven, this make the present invention compared with prior art the structure and making of equipment greatly simplify.Zosel and Wanzinski technology are provided with capital well heater and heat exchanger.
The mode that supercutical fluid of the present invention enters extraction section is to enter by " way flow " sparger, petroleum heavy oil, particularly not only viscosity is big for the extracted residues of petroleum residual oil, and softening temperature is also high, adopt the advantage of " way flow " sparger to be: can prevent that extracted residues from blowing back into solvent line and causing the fault of line clogging to take place, assurance separation test safety is carried out smoothly.
The present invention can cut into a fraction arbitrarily with product according to the needs of petroleum heavy oil separate evaluation, and US4290880 and JP61-254693 can not be like this.
The present invention cools off through water cooler 7 at the effusive supercutical fluid in extraction and fractionation column top, avoided using not only heatproof but also withstand voltage, be difficult to satisfactory to both parties pressure regulator valve, and become highly pressurised liquid after the supercutical fluid cooling, it has bigger solvent ability, can avoid flowing out the residual solute of separating out of pipeline.
Pressure-controlling of the present invention adopts stepper motor driven needle-valve of microcomputer control to realize the purpose that linearity is boosted, this has following advantage than available technology adopting pressure-regulator Controlling System pressure: the control that makes linearity boost is simple and reliable, equipment configuration is simple, ILS, can realize accurately and intuitively control, in case of necessity, also can realize multiple boosting mode.
Adopt the present invention to separate petroleum heavy oil in a word and have the product yield height, the advantage of good separating effect, with grand celebration vacuum residuum is example, one kilogram of residual oil is packed in the extraction kettle of supercritical fluid extraction fractional column, and at the bottom of the still 220 ℃, 230 ℃ on capital, solvent flux 100ml/ branch (liquid), in 7 hours 20 minutes pressure is risen to 12.0MPa from 4.8MPa, grand celebration vacuum residuum can be separated into 17 close-cut fractions, total recovery can reach 89.2%.
With iC
4Being solvent, is raw material with triumph vacuum residuum, and separating resulting of the present invention and flushed in liquid phase chromatography result are relatively seen the following form:
Present method and flushed in liquid phase chromatographic separation result's comparison
By the visible two kinds of method nickel removal rates of table with to take off the carbon residue rate roughly the same, proof the present invention has separating effect preferably, and that the present invention has overcome aforesaid chromatography separation method is loaded down with trivial details, the gained sample size is few, be difficult to satisfy necessary various basic datas and information on the engineering, the too wide in the gap shortcoming that is unfavorable for using production practice of separation principle and production process, thereby has good separating effect, close-cut fraction cutting handiness is strong, each sample size is many, process is simple, again near the characteristics of production practice.
Accompanying drawing 1 is the tripping device schematic flow sheet.
Accompanying drawing 2 is supercutical fluid " single-phase flow " sparger synoptic diagram.
Accompanying drawing 3 is the Controlling System block diagram.
The present invention is further illustrated below in conjunction with accompanying drawing:
See accompanying drawing 1, with separated raw material, petroleum residual oil for example is through head tank 31 and feedstock pump 32, by the valve 33 disposable extraction stills 1 of sending into the supercritical fluid extraction still. The raw material amount of sending into is by electronic scale 30 meterings. The lighter hydrocarbons solvent is with the flow velocity of per minute 60 to 200 milliliters (liquid), from the bottom of solvent tank 20, through valve 24, filter 25, be pressurized to the critical pressure that is higher than solvent through solvent pump 26 again, and the numeral of flowing through shows that flowmeter 27 and valve 28 enter the electrothermal solvent and give hot stove 29. The supercritical fluid that is heated to above 10 to 50 ℃ of solvent critical-temperatures (being measured by proof armored platinum resistor thermometer 6-6) enters the extraction still from extraction still 1 bottom " way flow " the formula supercritical fluid distributor 3 of supercritical fluid extraction still bottom, fully contacts with separated raw material 2. Under the supercritical temperature of solvent, pressure condition, extract, form two-phase. The supercritical fluid that the is dissolved with part material packing layer 5 of flowing through in opposite directions. Filler can be the Stainless Steel θ ring filler of φ 2 * 2mm. Whole extraction and fractionation post adopts three sections electric heating thermal insulations and heating, and the temperature of the supercritical fluid phase of the filling batch of flowing through is progressively raise, and keeps filling batch that uniform thermograde is arranged. The each point temperature is respectively by proof armored platinum resistor thermometer 6-1,6-2, and 6-3 and 6-4 measure. The temperature difference of 6-4 and 6-1 is 10 to 80 ℃, and two-phase temperature 6-1 and 6-2 in the extraction still 1 are basic identical. Because upwards flowing through the supercritical fluid phase temperature of filling batch progressively rises Height, the density of supercritical fluid also will reduce gradually, and its solvent ability is descended, and the dissolved raw material of part is separated out downward inflow packing layer and is formed backflow. What happens is the same in the like destilling tower, and the supercritical fluid phase of rising is carried out transmission and the exchange of quality and energy with backflow in filling batch, thereby realizes the purpose of extraction and fractionation. The supercritical fluid that flows through filling batch is decompressed to 0.2 to 2.0MPa from flow through cooler 7 and pressure-regulating valve 9-1 of column top outlet, and whether the observation window 12(that flows through can observe separation test normal), enter solvent product separator 14-1. By electrothermal solvent product separator heating furnace 14-2, when low pressure solvent product mixture is heated to 100～200 ℃ (being measured by proof armored platinum resistor thermometer 6-5), can substantially realize both fully separation. The product that contains a small amount of solvent flows into sample divider 16 from valve 15, and its weight is by electronic scale 17 meterings. Product after trace solvent is removed in vacuum drying, is measured various physicochemical properties again. Do not contain the solvent of product after solvent condenses cooler 18 is chilled to room temperature, enter solvent tank 20 through valve 19 and recycle. The solvent tank height of liquid level is observed by liquid level gauge 21. Be filled with an amount of nitrogen by nitrogen cylinder 34 through valve 35 and keep the solvent tank stagnation pressure and be higher than solvent saturated vapor pressure 0.1-0.5MPa under the room temperature, run well to guarantee solvent pump. When solvent is not enough, can pass through pipeline 23 and valve 22 to system's supplementing solvent. System's each point temperature (6-1 to 6-6) is controlled by microcomputer.
In the process of the test, keeping under the constant condition of still each point temperature (6-1 to 6-4), by pressure-regulating valve 9-1 and stepper motor 9-2, by Control System of Microcomputer 10, the extraction and fractionation column pressure can be boosted in the lower linearity that realizes of the constant rate of rise (0.5 to 1.5MPa/hr). The pressure that raises gradually under the steady temperature, the solvent ability of supercritical solvent constantly strengthens, raw mix, petroleum residual oil for example, each cut will be separated successively by the size of its solubility. Told the number of narrow fraction and can be determined arbitrarily on demand example Can cut by accounting for raw material 5% such as each narrow quantity of heating up in a steamer, so can also obtain the relation between productive rate and the pressure.
Separation test can pass through valve 36 nitrogen blowing experimental rig after finishing, and waste gas is from valve 37 emptying.
Accompanying drawing 2 is " way flow " distributor, comprises a limit screw cap 1, the cone 2 of floating and base 3.
Explain below in conjunction with 3 pairs of pressure and temp control systems of accompanying drawing:
Whole device is controlled in real time by an IBM286 microcomputer. Microcomputer dominant frequency 16MHZ, internal memory 1MB is equipped with 40MB hard disk and high resolution colour display screen. Microcomputer is controlled by given process conditions installing upper each point temperature and pressure, and on screen, dynamically show in a flowchart the variation of each point parameter, simultaneously can real time print each point parameter, preserve as record, can also check in case of necessity the each point parameter historical variations trend that represents with curve, given full play to computer-controlled fast, accurately, intuitively, characteristics flexibly.
Another characteristics of this control system are that the LINEAR CONTINUOUS that adopts stepper motor to drive in the needle-valve realization low discharge experimental provision is boosted. Facts have proved that this scheme is successful.
The importation: totally 9 of temperature sensors 1, all adopt precision height, proof armored platinum resistor thermometer that repdocutbility is good. It is the PTV-1 type piezoelectric transducer of 0.2FS that pressure sensor 2 adopts precision. The signal of sensor output passes through respectively signal conditioning circuit 3,4 separately, telecommunications is adjusted into 0～10V, the data acquisition in cable is delivered to computer and interface board.
Multiple signals convert digital quantity to by Multipexer journey switch 5 and sample/hold circuit 6 and A/D converter 7 and enter computer 8 and process. Here the critical component A/D converter adopts 12 high accuracy chip AD574, has guaranteed the requirement of control accuracy.
Output: after the as calculated machine contrast of said temperature, pressure signal, calculating, the processing (calculating comprising digital PID), provide control signal, control each heater and pressure-regulating valve.
Temperature control is the make-and-break time that computer 8 passes through timer 9 control solid-state relays 10, thus length heat time heating time of control heater 11. Solid-state relay is zero-based, photoelectric coupling, and TTL is moving the driving directly, and is easy to use and reliable, and can reduce the interference of other circuit of higher hamonic wave. Temperature control loop has 5.
Pressure control is adopted stepper motor 15 to drive needle-valve 16 and is regulated. The time that computer is controlled the motor forward or reverse by timer 12 realizes controlling the open and close of needle-valve, reaches the purpose of controlled pressure. At the pressure control section, for making stepper motor normal operation, cycle pulse distributor 13 big-power rectification power supplies 14 that produce clock pulse and limit switch etc. must be arranged.
In the block diagram, 17,18,19 are respectively high resolution color display, printer and keyboard.
Below enumerate embodiment the present invention is done progressive step explanation, solvent for use is the commercial goods among the embodiment.
Squeeze into 1000g grand celebration long residuum in the extraction kettle of separator column bottom by the raw material sampling pump, keep at the bottom of the still 110 ℃ of temperature, 130 ℃ of column top temperatures, under the petrogas flow of 90ml/min, make the extraction and fractionation column pressure boost to 12.0MPa by pressure control system by the 4.5MPa linearity, and maintenance rate of rise 0.75MPa/hr, can extract the grand celebration long residuum out 15 close-cut fractions (seeing the following form) by the difference of character, each close-cut fraction yield is about 5%, total sucrose extraction 76%(m), keeping product separated from solvent actuator temperature is 150 ℃, and pressure 1.5MPa can make product effectively be separated with solvent.
Normal slag of grand celebration and close-cut fraction character
The separation of triumph vacuum residuum, process is with example 1.
Solvent: iC
4Cut (iC
481.8%, nC
413.3%)
Temperature at the bottom of the still: 145 ℃
The extraction and fractionation column temperature is poor: 18 ℃
Pressure range: 4.0-12.0MPa
The rate of rise: 1.0MPa/hr
Solvent flux: 75ml/min(1)
Raw material add-on: 1500g
Extract total recovery out: 63.3%(m)
Close-cut fraction number: 14
The separation of grand celebration vacuum residuum, process is with example 1.
Solvent: Skellysolve A
Temperature at the bottom of the still: 230 ℃
The extraction and fractionation column temperature is poor: 10 ℃
Pressure range: 4.5-12.0MPa
The rate of rise: 0.85MPa/hr
Solvent flux: 93ml/min(1)
Raw material add-on: 800g
Extract total recovery out: 89.8%(m)
Close-cut fraction number: 18
The separation of isolated island vacuum residuum, process is with example 1.
Solvent: Skellysolve A
Temperature at the bottom of the still: 230 ℃
The extraction and fractionation column temperature is poor: 10 ℃
Pressure range: 4.5-12.0MPa
The rate of rise: 0.9MPa/hr
Solvent flux: 90ml/min(1)
Raw material add-on: 800g
Extract total recovery out: 82%(m)
Close-cut fraction number: 17
Claims (3)
1, a kind of method of separating petroleum heavy oil is characterized in that: mink cell focus is sent in the extraction kettle 1 of supercritical fluid extraction fractional column, with C
3, C
4, nC
5Or its mixture is a solvent, supercharging heats to being higher than its emergent pressure and critical temperature, makes supercutical fluid enter extraction kettle 1 from " way flow " formula supercutical fluid sparger 3 of supercritical fluid extraction fractional column bottom, fully contacts with raw material, extract, form two-phase; The supercutical fluid that is dissolved with part material is flowed through in opposite directions and is raise to going up temperature down, and filling batch 5 with constant temp gradient, bed temperature is 100-250 ℃, make the dissolved raw material of part separate out downward inflow packing layer and form backflow, the pressure of extraction and fractionation post adopts linear boosting mode during separation, pressure can be 3.5-20MPa, and rate of rise 0.5-1.5MPa/hr realizes extraction and fractionation; The supercutical fluid that flows through filling batch is from column top spout flow through water cooler 7 and pressure regulator valve 9-1, enter solvent product separator 14-1 after being decompressed to 0.2-2.0MPa, electrically heated is to 100-200 ℃, realize the separation of the two, product cuts into any fraction by the size of molecular weight, collects vacuum-drying by collector 16, solvent uses through refrigeration cycle, can replenish when solvent is not enough.
2, according to the method for claim 1, it is characterized in that: the temperature of extraction and fractionation post has the constant temp gradient, its extraction kettle temperature is higher than 10-50 ℃ of solvent critical temperature, column top temperature is higher than at the bottom of the post temperature 10-80 ℃, the flow rate of circulating solvent is 60-200ml/ branch (liquid), and the filler of filling batch can be selected the stainless steel θ ring filler of φ 2 * 2mm for use.
3, a kind of supercritical fluid extraction fractionation plant that separates petroleum heavy oil, comprise: the raw material fresh feed pump, high-pressure solvent pump, the solvent preheating oven, the supercritical fluid extraction fractional column, the solvent product separator, the solvent cylinder, the supercutical fluid water cooler, solvent condenses water cooler and temperature, pressure calculate the machine Controlling System, it is characterized in that the extraction and fractionation post is divided into extraction kettle and fractionation section two portions, are equipped with one in the extraction kettle bottom and can prevent that extracted residues from blowing back into " way flow " supercutical fluid sparger of solvent line, this sparger comprises a limit screw cap, unsteady cone and base; The heating unit that the extraction and fractionation post adopts is three sections electrically heated, by microcomputer control, to realize the extraction and fractionation post uniform temperature gradient is arranged, and realizes that with micro-processor controlled stepper-motor drive needle-valve the linearity of extraction and fractionation post boosts.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93117577 CN1031800C (en) | 1993-09-24 | 1993-09-24 | Method for separating petroleum heavy oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93117577 CN1031800C (en) | 1993-09-24 | 1993-09-24 | Method for separating petroleum heavy oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1083513A true CN1083513A (en) | 1994-03-09 |
| CN1031800C CN1031800C (en) | 1996-05-15 |
Family
ID=4992089
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 93117577 Expired - Fee Related CN1031800C (en) | 1993-09-24 | 1993-09-24 | Method for separating petroleum heavy oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1031800C (en) |
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| WO2010037350A1 (en) * | 2008-09-27 | 2010-04-08 | 广东省电力设计研究院 | Method of physicochemical treatment for waste water of orimulsion oil |
| WO2011113225A1 (en) * | 2010-03-15 | 2011-09-22 | Peking University | Extraction of a component from a composition using supercritical fluid |
| CN102565117A (en) * | 2012-01-18 | 2012-07-11 | 辽宁同辉科技发展有限公司 | Device for quantitatively measuring components in coking crude benzene by distillation drop method |
| CN102565118A (en) * | 2012-01-18 | 2012-07-11 | 辽宁同辉科技发展有限公司 | Distillation temperature tracker and distillation temperature tracking method thereof |
| CN102590440A (en) * | 2012-01-18 | 2012-07-18 | 辽宁同辉科技发展有限公司 | Quantitative determination method for component distillation drops of coking crude benzol |
| CN102584643A (en) * | 2011-01-13 | 2012-07-18 | 中国石油大学(北京) | Crude oil vacuum residue fraction sulfonate and preparation method thereof |
| CN103059921A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Heavy oil separation method |
| CN105400545A (en) * | 2014-09-10 | 2016-03-16 | 中国石油大学(北京) | Heavy oil separation method and treatment system thereof |
| CN105447290A (en) * | 2014-08-19 | 2016-03-30 | 徐大鹏 | Evaluation method for heavy petroleum oil separation by supercritical fluid extraction and fractionation |
| CN107604161A (en) * | 2017-08-01 | 2018-01-19 | 苏州市文益石油化工有限公司 | A kind of diluent for being used for rare earth and rare precious metal liquid extraction and preparation method thereof |
| CN108883382A (en) * | 2016-02-19 | 2018-11-23 | 林德股份公司 | Method and apparatus for obtaining the ethylene product of supercriticality |
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1993
- 1993-09-24 CN CN 93117577 patent/CN1031800C/en not_active Expired - Fee Related
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| WO2010037350A1 (en) * | 2008-09-27 | 2010-04-08 | 广东省电力设计研究院 | Method of physicochemical treatment for waste water of orimulsion oil |
| WO2011113225A1 (en) * | 2010-03-15 | 2011-09-22 | Peking University | Extraction of a component from a composition using supercritical fluid |
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