CN1347442A - Improved process for deasphalting residue by reactive recycle for high boiling material - Google Patents
Improved process for deasphalting residue by reactive recycle for high boiling material Download PDFInfo
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- CN1347442A CN1347442A CN 00806321 CN00806321A CN1347442A CN 1347442 A CN1347442 A CN 1347442A CN 00806321 CN00806321 CN 00806321 CN 00806321 A CN00806321 A CN 00806321A CN 1347442 A CN1347442 A CN 1347442A
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- steam
- residence time
- solid
- conversion zone
- soaking drum
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
- C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Working-Up Tar And Pitch (AREA)
Abstract
The vaporized fraction is passed via line (11) to soaker drum (2) which is maintained at effective conditions so that the highest boiling materials are condensed out. Typically these conditions will include controlled quenching of vapor fraction just below the dewpoint. A quench stream can also be passed into soaker drum via line (21).
Description
Invention field
The present invention relates to a kind of use moves horizontally short steam residence time process unit that bed forms by the hot particulate of fluidizing and/or stirring and makes that residual oil raw material is deasphalting improves one's methods.The vapor phase product stream that described process unit obtains is sent into soaking drum, cause there after the reaction of molecular weight increase, isolate high boiling fraction and recirculation and return described process unit.Compare with the liquid product quality that one-pass residual oil deasphalting method alternative obtains, use this reaction recirculation of soaking drum that the quality of liquid product is improved greatly.
Background of invention
In a typical refinery, crude oil distills through normal pressure, isolates lighter material from heavier material, for example gas oil, kerosene, gasoline, virgin naphtha etc.Then the residual oil that obtains in the air distillation step is under reduced pressure distilled.This back one distilation steps obtains vacuum gas oil fraction oil and vacuum residuum, and the latter is usually contained quite high-load asphaltene molecules.These asphaltene molecules contain the most of Conradson carbon residue and the metal component of residual oil usually.They also contain high-load relatively heteroatoms, for example sulphur and nitrogen.Such raw material has very little commercial value, mainly is because more and more stricter environmental regulations makes them can not be used as oil fuel.They as the various technological processs of refinery for example the raw material of fluid catalytic cracking also have very little value because they produce excessive coke and gas.In addition, their high metal content also makes catalyst deactivation.Therefore, in refining of petroleum, very the resid feed upgrading need be become more valuable, more cleaning and lighter charging.
There are many technology to be used for reclaiming lighter component from various pitch petroleum residual oil chargings.Many such methods comprise with the deasphalting solvent lighter component of propane extraction for example, separate from solvent then and reclaim lighter component.In US 2950244, the method that a kind of extraction contains the bituminous petroleum residual oil is disclosed.Used solvent for through liquefaction be generally the gasiform solvent, propane for example is maintained at about 100 to 200 °F and be enough to make this solvent to remain under the pressure of liquid phase with it.
The U.S.4201660 that June 23 in 2669538,1970 was presented to U.S.3516928, the U.S.4017383 that was presented to Beavon on April 12nd, 1977 of King etc. and was presented to Szosel on May 6th, 1980 at the US that is presented to Yuraski etc. disclose use propane or similarly short-chain fat family hydrocarbon as the various work-around solutions of the deasphalting method of solvent.King etc. also propose, and in some cases, carbonic acid gas and ammonia and low-carbon alkanes, alkene and halo derivatives thereof are solvents of equal value.
Though propane usually is used for traditional solvent deasphalting operation, has also proposed other solvents.For example, in U.S.4054512, contact with liquid hydrogen sulfide by bitumeniferous mineral oil and to make this oil product diasphaltene.In U.S.3334043, disclose at 0 to 250 °F and used the liquid neopentane down.In addition, in U.S.2337448, make the heavy oil residue diasphaltene with the solvent that is selected from ethane, ethene, propane, propylene, butane, butylene, Trimethylmethane and composition thereof.
The U.S.4191639 that is presented to Audeh etc. discloses a kind of like this method, wherein by be selected from hydrogen sulfide, carbonic acid gas and propane in the liquid mixture of at least two components contact and make hydrocarbon ils for example petroleum residual oil diasphaltene and demetalization.
In addition, U.S.5714056 also discloses and has a kind ofly made the residual oil deasphalting method in short steam thermal technique device duration of contact of the horizontal moving bed composition of the hot particulate of fluidizing.This is a kind of single pass method, thus the charging pollutent remove the restriction that is subjected to once by the decreasing ratio that can reach.Not mentionedly from the steam product cut, separate high boiling fraction and make it be recycled to conversion zone.
Though solvent deasphalting has been obtained business success, but still the de-asphalting method of higher liquid yield and Geng Gao liquid product quality need be arranged than solvent deasphalting.Need also under the condition of not using solvent, to make that bitumeniferous residual oil raw material is deasphalting improves one's methods.
Abstract of invention
According to the present invention, provide a kind of asphalt bearing stocks deasphalting method that in by the following diasphaltene process unit of forming, makes: (i) heating zone, contain the sedimental solid of carbonaceous what this received stripping stage, and can contain useful
There is heating down in heated air in partially combusted oxygen; (ii) short steam residence time conversion zone, it contains the circulation of fluidizing and/or stirring from heating zone
Hot solids move horizontally bed and charging, described conversion zone is about 450 to about 700
℃ and such condition under operate so that solid retention time and steam residence time are by solely
On the spot control, described steam residence time is less than about 5 seconds, and described solid is when stopping
Between be about 5 to about 60 seconds; And (iii) stripping stage, have to contain the solid that the carbonaceous settling is deposited on and pass through through it from conversion zone, its
In more lower boiling hydro carbons and volatile matter reclaimed by stripping gas; Described method comprises:
(a) residual oil raw material is sent into short steam residence time conversion zone, there it and hot consolidating
Body contacts with vaporised fraction, thereby makes high Conradson carbon residue component and metallic component deposition
On described hot solids;
(b) from solid, isolate vaporised fraction; And
(c) solid is passed through described stripping stage, they contact with stripping gas there, from
And therefrom remove volatile constituent;
(d) send into heating zone through steam stripped solid, they are heated to the maintenance conversion zone there
The significant temp of service temperature;
(e) hot solids is recycled to conversion zone from heating zone, and they contact with fresh feed there;
(f) vaporised fraction of above-mentioned steps (b) is sent into soaking drum, there its warp
It is about 450 that chilling generates steam cut and the initial boiling point that boiling range is lower than about 450-600 ℃
High boiling fraction condensation product to 600 ℃;
(g) in soaking drum, provide the enough residence time and reactor severity, make branch
The son amount increases reaction and produces;
(h) described high boiling fraction is recycled to short steam contact time reaction section; And
(i) reclaim the steam cut that low Pollutant levels are arranged from step (h).
In the present invention's one embodiment preferred, with water vapor, C
4 -Gas or both are injected in the soaking drum, solid are remained in the suspension and stripping goes out the product of low boiling range.
In another embodiment preferred of the present invention, soaking drum is operated under high pressure and high temperature, so that the reaction times is shortened, thereby the size of soaking drum is dwindled.
In the present invention's one embodiment preferred, the particle of short contact time reactions section is by mechanical means fluidisation and/or stirring.
In another embodiment preferred of the present invention, with water vapor, C
4 -Gas or both inject the vaporised fraction of soaking drum upstream, so that reduce C
5 +The dividing potential drop of hydro carbons, thus the high boiling fraction in the step of making (f) is being lower than condensation under about 450 to 600 ℃ initial boiling point.
In another embodiment preferred of the present invention, in soaking drum, there is polymerization starter, so that improve speed of reaction.
In another embodiment preferred of the present invention, soaking drum can be equipped with the mechanical mixing equipment that the automatically cleaning benefit is provided, so that make deposits of coke minimum and make liquid phase reach the plug-flow reaction condition basically.
The accompanying drawing summary
Unique accompanying drawing is the block diagram of the unrestriced preferred embodiment of the present invention.
Detailed Description Of The Invention
According to the residual oil raw material of upgrading of the present invention be boiling point surpass about 380 ℃, preferably surpass about 540 ℃, more preferably surpass about 560 ℃ petroleum fractions.The non-limitative example of such cut comprises vacuum residuum, long residuum, heavy topped crude, tar-bitumen, waste oil, petroleum pitch, pitch, solvent deasphalting residual oil and tar sand oil.Should be appreciated that such residual oil also can contain on a small quantity than low-boiling point material.Such raw material can not be sent into refinery process unit in a large number, FCC apparatus for example, because they have high Conradson carbon residue usually, and they also contain the metallic components of undesirable quantity usually.Conradson carbon residue is deposited on the FCC cracking catalyst, and causes the over-drastic inactivation.Metal for example nickel and vanadium also makes catalyst deactivation as catalyzer poison.The Conradson carbon residue content typical case of such charging is at least 5% (weight), is generally about 5 to 50% (weight).Test D189-165 about Con. carbon referring to ASTM.
According to the present invention, residual oil raw material is upgrading in so short steam residence time process unit, and described process unit is made up of the horizontal fluidised and/or teetered bed conversion zone and the stripping stage of heating zone, short steam residence time.Referring now to unique accompanying drawing, the residual oil raw material of wherein high Conradson carbon residue and/or high metal component is sent into one or more short steam residence time conversion zones 1 through pipeline 10, the latter have fluidizing and/or stirring hot solids move horizontally bed.Preferably will lack solid fluidisation and/or stirring in the steam residence time reactor by mechanical means.Reactor can be with stripping gas for example water vapor or C
4 -Gas or the steam stripped that produces with some feedstock fraction vaporizations.Preferred mechanical equipment is a kind of automatically cleaning mechanically mixing system, it is characterized in that having high relatively radially mixing efficiency, has only a spot of axial backmixing.Such mixed system resembles the piston flow system of such flow pattern, and this flow pattern can guarantee that all particulate residence time are almost equal.Most preferred mechanical mixer is the mixing tank that German LURGI proposes, and as LR-Mixer or LR-Flash Coker, they are used for treated oil page or leaf charcoal, coal and oil-sand originally.LR-Mixer is made up of the rotary screw of two or more horizontal alignments, and they mix charging and hot solids, stirs simultaneously and carries mixture by reactor.Though preferred solid particulate is a coke granule, they also can be other any suitable refractory particle materials.The unrestricted example of the infusibility material that like this other are fit to comprises that those are selected from silicon oxide, aluminum oxide, zirconium white, magnesium oxide, high red aluminium stone, synthetic or naturally occurring material, for example material of float stone, carclazyte, diatomite, bauxite etc.These solids are inert or have catalytic performance all within the scope of the invention.The solid mean particle size is preferably about 40 to 2000 microns, more preferably from about 200 to about 1000 microns.
Raw material and solid about 450 to about 700 ℃, preferred about 500 to 600 ℃, more preferably from about contact under 520 to 600 ℃.When this contact took place, the high Conradson carbon residue of the overwhelming majority and metallic component were deposited on the solid particulate of heat with the form of polymer charcoal and metal part.Rest parts is vaporized when contacting with hot solids.The residence time of steam product in conversion zone 1 is the time of such significant quantity, so that significant second pyrolysis does not occur.This time usually less than about 5 seconds, preferably less than about 2 seconds.The residence time of solid in conversion zone is about 5 to 60 seconds, preferred about 10 to 30 seconds.A novel aspect of the present invention is that solid and the steam product residence time in conversion zone is independently controlled.Most of fluidized bed processes are design so all, so that solid retention time and steam residence time can not be controlled independently, particularly under short relatively steam residence time, preferably, operation like this, short steam residence time process unit, thus the ratio of solid and charging is about 30/1 to 3/1, preferred about 5/1.Should be appreciated that the solid and the accurate ratio of charging depend primarily on the thermal equilibrium needs and the solid temperature of short steam residence time conversion zone.It is in the skill of being familiar with these professional those skilled in the art that oil need be combined than with thermal equilibrium with solid, does not therefore need to do any detailed description further here.A spot of raw material is deposited on the solid with the form of combustible carbonaceous material.Metal component also is deposited on the solid.Its result compares with original charging, and the part of vaporization has significantly low Conradson carbon residue and metal.
Vaporised fraction is sent into soaking drum 2 through pipeline 11, and the latter remains under such condition for validity, so that the material of maximum boiling point condenses.Usually these conditions comprise the just controlled chilling below dew point of steam cut.Condensation product keeps one period working lipe and reaction severity in soaking drum, so that initiated polymerization generates coke precursors.The chilling logistics also can be sent into soaking drum through pipeline 21.The chilling logistics is generally petroleum naphtha (C
5/ 150 ℃) to (550 ℃ of residual oil logistics
+) oil stream.Preferred chilling logistics is that boiling range is 300-700 ℃ a separation column bottoms.Coke or comprise that the polymerization starter that is selected from elementary sulfur, superoxide and waste cracking catalyst can be added in the soaking drum through pipeline 19.Water vapor, C
4 -Cut, air or its mixture also can be used for soaking drum, to improve the low component and make solid suspension in slurries of boiling of speed of reaction, stripping.In addition, soaking drum can make deposits of coke minimum continuously with the mechanical means cleaning.
Soaking drum was operated under the efficient temperature and the residence time, so that cause pyrogenic reaction, but did not reach a large amount of degree that generate deposits of coke in soaking drum.Preferred condition comprises about 350 to about 520 ℃, preferred about 400 to about 450 ℃ temperature and about 1 to 60 minute, preferred about 5 to 30 minutes residence time, and to take off pollution rate relevant with the character of charging and required charging for it.Suitably use soaking drum and will only make the steam product selectivity condensation of maximum boiling point and generate prepolymerized mink cell focus, it is recycled to conversion zone 1 through pipeline 9.This just makes metal removal rate bring up to this elimination round-robin 95% or higher from one-pass about 90%.The application of soaking drum also makes for example decreasing ratio raising of Conradson carbon residue, sulphur and nitrogen of other charging pollutents.Therefore, the quality of the liquid product that obtains significantly improves, and as the charging of refinery conversion process higher value is arranged.
The steam cut of soaking drum 2 is sent into cyclonic separator 20 through pipeline 14, removes most of entrained solid or dust there.To send into quench zone 13 through pipeline 24 through dust separating steam then, there the temperature of steam be reduced to below the temperature that remarkable thermo-cracking occurs.This temperature preferably is lower than about 450 ℃, more preferably less than about 340 ℃.There is carbonaceous material to deposit superincumbent solid and delivers to solid bed 17 stripping tower 3 from conversion zone 1 through pipeline 15.Solid is downwards by stripping tower, and the stripping stage by tower bottom, any there left volatile matter or vaporizable material stripping gas preferably water steam stripping from solid of introducing stripping stages through pipeline 16.Upwards send into quench zone 13 through steam stripped steam product in stripping tower 3, lighter products is removed through pipeline 28 as overhead materials there.Lighter products is generally 550 ℃
-Product stream.550 ℃
+Logistics is also collected from quench zone through pipeline 26.Deliver to the well heater 4 of heating zone through pipeline 18 through steam stripped solid.Heating zone is operated under significant temp in oxidizing gas environmental optimization air.Just under the temperature of the thermal equilibrium needs that satisfy conversion zone, operate.Heating zone is surpassing about 40 to 200 ℃ of the service temperature of conversion zone 1, preferred about 50 to 175 ℃, is more preferably from about operating under 50 to 120 ℃ the temperature usually.Should be appreciated that and the air through preheating can be sent into well heater.Though some carbonaceous residue are burnt from solid in heating zone, preferably only carry out partial combustion, so that still have the value that acts as a fuel by solid after the well heater.Excessive solid can be removed from process unit through pipeline 50.Fuel gas is removed as overhead materials from well heater 4 through pipeline 40.Fuel gas is through cyclonic separator 36,39 and 38, so that remove most of solid fines.Send into CO (carbon monoxide converter) boiler through dust separating fuel gas, be used for reclaiming the used heat (not shown), remove pollutent and particle, drain into atmosphere again through washing.Right gas is recycled to heat scission reaction section 1 with the inert solid of heat through pipeline 12.
Claims (15)
1. one kind makes bitumeniferous raw material deasphalting method in by the diasphaltene process unit of forming with the lower section: (i) heating zone contains the sedimental solid of carbonaceous what this received stripping stage, and is useful on can containing
There is heating down in the heated air of partially combusted oxygen; (ii) short steam residence time conversion zone, it contains from the hot solids of heating zone round-robin through stirring
Move horizontally bed and charging, described conversion zone is at about 450 to about 700 ℃ and like this
Condition under operate so that solid retention time and steam residence time be independently controlled,
Described steam residence time is less than about 5 seconds, and described solid retention time be about 5 to
About 60 seconds; And (iii) stripping stage, deposit superincumbent solid by should from the carbonaceous of the containing settling that has of conversion zone
Stripping stage reclaims more lower boiling hydro carbons and volatile matter with stripping gas there; This method comprises: (a) resid feed is sent into short steam residence time conversion zone, there it and fluidizing and/or
The hot solids that stirs contacts with vaporised fraction, thereby makes high Conradson carbon residue component and containing metal
Component be deposited on the described hot solids;
(b) vaporised fraction and solids constituent from; (c) solid is sent into described stripping stage, they contact with stripping gas there, thereby therefrom
Remove volatile constituent; (d) will send into heating zone through steam stripped solid, there they will be heated to the operation of maintenance conversion zone
The significant temp of temperature;
(e) hot solids is recycled to conversion zone from heating zone, and they contact with fresh feed there; (f) vaporised fraction of above-mentioned steps (b) is sent into soaking drum, it is by chilling there,
The generation boiling point is lower than about 450 to 600 ℃ steam cut and initial boiling point is about 450 to 600 ℃
The high boiling fraction condensation product; (g) in soaking drum, provide the enough residence time and reactor severity, molecular weight is increased
Long reaction takes place;
(h) described high boiling fraction is recycled to short steam residence time conversion zone; And
(i) reclaim the steam cut that the low concentration pollutent is arranged from step (h).
2. according to the process of claim 1 wherein that the steam residence time of short steam residence time conversion zone was less than about 2 seconds.
3. according to the process of claim 1 wherein that residual oil raw material is selected from vacuum residuum, long residuum, heavy topped crude, tar-bitumen, waste oil, petroleum pitch, pitch, solvent deasphalting residual oil, tar sand oil.
4. according to the method for claim 3, wherein residual oil raw material is a vacuum residuum.
5. according to the method for claim 2, the solid retention time of its short-and-medium steam residence time conversion zone is about 10 to 30 seconds.
6. according to the process of claim 1 wherein that the particle of short steam contact time reaction section is by mechanical means fluidisation and/or stirring.
7. according to the method for claim 6, wherein mechanical means is made up of the screw rod of one group of horizontal positioned in reactor.
8. according to the process of claim 1 wherein that soaking drum operates under about 350 to 520 ℃ temperature and about 1 to 60 minute residence time.
9. method according to Claim 8, wherein soaking drum is operated under the pressure of about 1 to 10 crust.
10. according to the method for claim 9, wherein soaking drum is operated under the pressure of about 400 to 450 ℃ temperature and about 1 to 3 crust.
11. method according to Claim 8 wherein is added to polymerization starter in the soaking drum, to improve speed of reaction.
12. according to the method for claim 11, wherein polymerization starter is selected from elementary sulfur, superoxide, spent catalyst, coke granule and air.
13. according to the process of claim 1 wherein with water vapor, C
4 -, air or its mixture inject soaking drum stripping goes out low-boiling products so that make solid keep suspending also in slurries.
14. according to the process of claim 1 wherein that soaking drum can be such mechanical mixing equipment, it is with the piston stream mode operation and self-cleaning is provided, so that make deposits of coke minimum.
15. according to the process of claim 1 wherein with water vapor, C
4 -Gas or its mixture are added in the steam cut from the short residence time(SRT) conversion zone, make its branch drops and make the condensation of higher cut.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US29302999A | 1999-04-16 | 1999-04-16 | |
| US09/293,029 | 1999-04-16 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1347442A true CN1347442A (en) | 2002-05-01 |
Family
ID=23127326
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 00806321 Pending CN1347442A (en) | 1999-04-16 | 2000-04-11 | Improved process for deasphalting residue by reactive recycle for high boiling material |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP1194498B1 (en) |
| JP (1) | JP4590108B2 (en) |
| CN (1) | CN1347442A (en) |
| AR (1) | AR023503A1 (en) |
| AU (1) | AU771590B2 (en) |
| CA (1) | CA2370591C (en) |
| ES (1) | ES2559272T3 (en) |
| WO (1) | WO2000063320A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111201306A (en) * | 2017-09-12 | 2020-05-26 | 沙特***石油公司 | Integrated process for mesophase pitch and petrochemical production |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020038778A1 (en) | 2000-05-01 | 2002-04-04 | Maa Peter S. | Process for upgrading residua |
| US7033486B2 (en) | 2002-04-01 | 2006-04-25 | Exxonmobil Research And Engineering Company | Residuum conversion process |
| JP5239226B2 (en) * | 2007-06-28 | 2013-07-17 | 株式会社Ｉｈｉ | Heavy fuel reforming method and reformer |
| JP6852094B2 (en) * | 2016-06-14 | 2021-03-31 | ストーン，リチャード | Turbulent mesophase pitch process and products |
| US10508240B2 (en) | 2017-06-19 | 2019-12-17 | Saudi Arabian Oil Company | Integrated thermal processing for mesophase pitch production, asphaltene removal, and crude oil and residue upgrading |
| US10913901B2 (en) | 2017-09-12 | 2021-02-09 | Saudi Arabian Oil Company | Integrated process for mesophase pitch and petrochemical production |
| DE102018213210A1 (en) | 2018-08-07 | 2020-02-13 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. | Process for cleaning mineral solids and wood materials, device for this process and its use |
| KR102481197B1 (en) * | 2020-08-13 | 2022-12-27 | 최창균 | Source pitch continuous charging and reformed Precursor pitch continuous discharging device for Pitch Reforming Method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3334043A (en) * | 1965-09-29 | 1967-08-01 | Sun Oil Co | Neopentane separation of bituminous materials |
| US4054512A (en) * | 1976-10-22 | 1977-10-18 | Exxon Research And Engineering Company | Deasphalting with liquid hydrogen sulfide |
| US4191639A (en) * | 1978-07-31 | 1980-03-04 | Mobil Oil Corporation | Process for deasphalting hydrocarbon oils |
| US4277324A (en) * | 1979-04-13 | 1981-07-07 | Exxon Research & Engineering Co. | Treatment of pitches in carbon artifact manufacture |
| US5714056A (en) * | 1995-07-17 | 1998-02-03 | Exxon Research And Engineering Company | Process for deasphalting residua (HEN9511) |
-
2000
- 2000-04-11 JP JP2000612401A patent/JP4590108B2/en not_active Expired - Fee Related
- 2000-04-11 ES ES00925922.7T patent/ES2559272T3/en not_active Expired - Lifetime
- 2000-04-11 AU AU44542/00A patent/AU771590B2/en not_active Ceased
- 2000-04-11 EP EP00925922.7A patent/EP1194498B1/en not_active Expired - Lifetime
- 2000-04-11 CA CA2370591A patent/CA2370591C/en not_active Expired - Fee Related
- 2000-04-11 WO PCT/US2000/009607 patent/WO2000063320A1/en active Application Filing
- 2000-04-11 CN CN 00806321 patent/CN1347442A/en active Pending
- 2000-04-14 AR ARP000101746 patent/AR023503A1/en unknown
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111201306A (en) * | 2017-09-12 | 2020-05-26 | 沙特***石油公司 | Integrated process for mesophase pitch and petrochemical production |
| CN111201306B (en) * | 2017-09-12 | 2022-04-19 | 沙特***石油公司 | Integrated process for mesophase pitch and petrochemical production |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4590108B2 (en) | 2010-12-01 |
| AU771590B2 (en) | 2004-03-25 |
| CA2370591C (en) | 2011-01-11 |
| WO2000063320A1 (en) | 2000-10-26 |
| JP2002542375A (en) | 2002-12-10 |
| AU4454200A (en) | 2000-11-02 |
| CA2370591A1 (en) | 2000-10-26 |
| ES2559272T3 (en) | 2016-02-11 |
| EP1194498A1 (en) | 2002-04-10 |
| AR023503A1 (en) | 2002-09-04 |
| EP1194498A4 (en) | 2011-02-16 |
| EP1194498B1 (en) | 2015-11-11 |
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