CN101360807B - Method for distilling a hydrocarbon material and a plant for carrying out the method - Google Patents
Method for distilling a hydrocarbon material and a plant for carrying out the method Download PDFInfo
- Publication number
- CN101360807B CN101360807B CN200680051680.3A CN200680051680A CN101360807B CN 101360807 B CN101360807 B CN 101360807B CN 200680051680 A CN200680051680 A CN 200680051680A CN 101360807 B CN101360807 B CN 101360807B
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- Prior art keywords
- evaporator
- target product
- cyclone evaporator
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- grade
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- Expired - Fee Related
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/30—Fractionating columns with movable parts or in which centrifugal movement is caused
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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
- C10G7/00—Distillation of hydrocarbon oils
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The inventive method for distilling a hydrocarbon material is carried out on several dividing stages in cyclone evaporators with a heated cylindrical vertical wall. The inventive method consists in supplying the raw material heated to the initial boiling point of a first high-boiling fraction to the first stage evaporator, in removing a liquid phase therefrom in the form of a marketable product, in cooling a withdrawn vapour fraction to the lower boiling point of a subsequent phase, in directing said fraction for separation to a next evaporator and in obtaining therein a gasoline in the form of a vapour fraction and a distillation residue. The inventive plant for carrying out said method comprises in series connected by pipelines heat exchangers, a raw material heating stove and equipment for one or several distillation stages each of which comprises an evaporator, a cooler, heat exchangers and intermediate collecting containers for target products. Each evaporator is embodied in the form of a heat-insulated cyclone evaporator provided with a heated vertical cylindric wall. The cooler of each stage is embodied in the form of an air-and-water heater.
Description
Technical field
The present invention is related to that (little petroleum refinery (H ∏ 3) is gone up the processing of oil, to obtain motor spirit and boiler oil (gasoline, diesel oil, heavy oil) at little tonnage assembly apparatus.
Background technology
In the structural form of contemporary large-tonnage hydrocarbon material distillating method equipment, comprising: pump, heat exchanger, tube furnace, rectifying volumn.In principle, the process program of little tonnage topping plant is the same with similar large-tonnage device, and the characteristics of still-process equipment structural form are that metal wastage is high, and require a large amount of capital investments.
Consider the complicacy that the little tonnage installation cost of making by the little petrochemical complex of large-tonnage factory circuit is high and move, researching and developing the non-traditional process program of hydrocarbon material distillatory always, at first refusal adopts rectifying volumn.
The known method (Russ P No.2200182, on March 10th, 2003) that a kind of hydrocarbon material fore-running is arranged, in the method; Adopt phase cyclonic separator and contact evaporator; Become several cuts to separated from petroleum, and perhaps the continuous duty at device obtains gasoline fraction and the heavily loaded excess of sloughing gasoline; Perhaps the regular operating mode at device obtains gasoline fraction, diesel oil and boiler oil.In solid flow heat exchanger, heat raw material, in phase separator, separate into liquid phase and vapour phase.Get into the air space of contact evaporator with reflux type in the disperse state liquid phase.Additional heating vapour phase exceeds 30～50 ℃ of liquidus temperatures, delivers to the liquid phase space that is arranged in the contact evaporator lower region as vaporization agent through the bubbling divider, obtains gasoline fraction from vaporizer during the vapour phase condensation.In order to obtain diesel oil, go the gasoline resistates to circulate through vapour well heater and phase separator, its as a result superheated diesel oil vapour in contact evaporator, under 250～300 ℃ of temperature, be used for steaming boiler oil (raw material residual processing thing).
The shortcoming of currently known methods is: use cf-only is used for strengthening the separation of liquid and vapor capacity in phase separator, still, and in this case; Not that kind of being claimed passes through to utilize the lighting end superheated vapour that takes out; Liquid phase is steamed for three times, and the fuel fraction sharp separation is infiltrated by last running steam but lighting end three times has taken place; At this moment, liquid (last running) will increase lighting end.(∏ Д is listed as other Jeff, heat exchange, drying and refrigerating unit, Moscow to this classical law according to dalton and Pa Wula; Energy press, 1966, the 138-140 page or leaf); Be applicable to the last running vapour concentration that adopted often greater than the structure of the phase separator and the vaporizer of lighting end concentration (because in these containers; The last running liquid phase volume is fixed very), obtain when this means these vapour condensations: not gasoline, but the mixture of gasoline and rope grain oil; Not diesel oil, but the mixture of gasoline, kerosene and lubricating oil cut.These mixtures can not use as motor spirit.
In addition, use the phase centrifuge separator to also have one to reduce the significant drawback that hydrocarbon material is divided into several cut sharpness, Here it is because the work of expansion liquid-vapor mixture cools off, and at this moment, the condensation of part light oil distillate converts liquid phase to heavy oil fraction.Calculating shows that on the boiling point temperature scale, the cut width that the condensation of this scope is got off is about 2 ℃.In addition, the light oil distillate that produces many a times coagulates refrigerating loss and has gone to liquid phase, and this is because the thermosteresis of surrounding environment causes, even heat insulation extraordinary phase centrifuge separator-cyclonic separator is also like this.According to the difference of feed composition, total losses and can reach 5～10% to the influence of quality index,, this is very big numeral concerning petroleum industry.
By technical spirit and the result that reached, the method near the application is, the method described in the valid model certificate No.17004 (March 10 calendar year 2001) " the refining of petroleum station that multicomponent fractionation is used ".What distillation this currently known methods comprises; In implementation process; Be heated to fore-running boiling lower limit temperature to raw material, the liquid-vapor mixture of generation is delivered to the distillation level, separates into liquid and vapor capacity at each grade liquid-vapor mixture; Liquid distillate takes out as target product, and vapour phase is cooled to next cut boiling lower limit temperature.Last step distillatory vapour phase is condensed, and takes out as target product.
The shortcoming of currently known methods is impossible clearly separate into cut to component, this means to obtain qualified motor spirit, and its reason is: the liquid that a large amount of band heavy oil fractions is arranged in vaporizer; And the light oil distillate that enters into liquid-vapor mixture is seldom, but according to dalton be afraid of that (∏ Д is listed as other Jeff to the Pa Wula law, heat exchange, drying and refrigerating unit; Moscow, energy press, 1966; The 138-140 page or leaf), the heavy oil fraction vapour concentration on fluid surface top is higher than the light oil distillate vapour concentration in the vaporizer; This means when light oil distillate removes water cooler to also have a large amount of about heavy oil fractions, and; According to same dalton and Pa Wula law, the part light oil distillate is stayed in the liquid phase in the vaporizer.
Known have the distillation tertiary mixture device (∏. Д. be listed as other Jeff, heat exchange, drying and refrigerating unit, Moscow, energy press,, 151 pages, Fig. 5-11 in 1966).The distillation of condensing surface and two levels is arranged in this device, and wherein each level has still kettle, rectifying tower, fractionator, separator, mixture heating up device, component of mixture collection container.In each grade resistates of device, obtain containing the mixture of a large amount of high boiling components, and have part overhead product to get into the second stage than volatiles.In partial resistates, obtain other component, and evaporable gets into condensing surface in three components.
The shortcoming of above-mentioned known devices is that quality is heavy, bulky, because rectifying tower is the vertical type cylinder body of being processed by steel, the pig iron or pottery, it highly reaches 30 meters, and diameter is 5 meters.Such device can not move to the refining of petroleum place, and it can only be fixed on a local work.Known this device needs to use high-pressure water vapor, and this makes operation and safeguards more complicated.
Be refining of petroleum station (the Russian valid model certificate No.17004 that multicomponent distillation is used near the method for applying among this paper; March 10 calendar year 2001); It has petroleum mixture line of pipes and liquid distillate vent line; What distillation of petroleum mixture with pipeline is connected in series has condensing surface, the petroleum mixture well heater in each level; Being installed in series, (it is knockdown petroleum mixture recuperative heater and water cooler, also has pump and petroleum mixture to heat the stove of usefulness for heat exchanger on the petroleum mixture intake pipeline.The distillation of each grade of petroleum mixture all is equipped with the vaporizer with built-in petroleum mixture well heater, and it makes the form of stove hall, is used for combustion of liquid or geseous fuel.
The shortcoming of this device is in device, can not clearly be divided into cut to component, this means to obtain qualified motor spirit (gasoline and diesel oil).Its reason is: the liquid of a large amount of band heavy oil fractions is arranged in vaporizer, and the light oil distillate that enters into liquid-vapor mixture seldom.But according to dalton and Pa Wula law, the heavy oil fraction vapour concentration on fluid surface top in the vaporizer is with municipal administration ground light oil distillate vapour concentration; This means; When light oil distillate removes water cooler, also have a large amount of heavy oil fractions, and; According to same dalton and Pa Wula law, the part light oil distillate is stayed in the liquid phase in the vaporizer.Certain liquid level leans on the work of valve system to keep in the vaporizer, discharges superfluous generation liquid through valve.Obviously, because the working result of such valve system will obtain gasoline, diesel oil and very small amount of heavy oil.
Summary of the invention
The main task of the one group of invention that proposes is to confirm hydrocarbon polymer distillatory method, sets up the device of implementation method, on compact and device that volume is little, obtain high-quality petroleum products.
The way that solves proposing of task is: the distillating method including what distillatory hydrocarbon material is; Be heated to raw material the lower limit of fore-running boiling point; Deliver to the distillation level to the liquid-vapor mixture that generates; Separate into liquid and vapor capacity at each grade liquid-vapor mixture, discharge liquid phase, and vapour phase is cooled to next cut boiling point lower limit as target product.
Novel is: on all levels of distillatory, isolating liquid and vapor capacity, all be on the cyclone evaporator that has the vertical type cylinder body wall, to carry out, and the vertical wall of each vaporizer all heats.
Preferably, target product is from the outlet position that cyclone evaporator comes out, and floor surface should be not less than target product most probable position in interceptor(-ter) relatively, and target product gets into the inlet of interceptor(-ter), should be lower than the minimum possible position of target product.
The power of each cyclone evaporator vertical type cylinder body wall heating is preferably controlled to such an extent that make liquid-vapor mixture equal vapour phase in the local temperature of cyclone evaporator outlet in the temperature of cyclone evaporator inlet.
The most handy controllable airflow of the cooling of vapour phase carries out.
Quantity by the resulting target product cut of boiling point equals n+1, and here, n is the quantity of cyclone evaporator.
Solving proposing of task also passes through: raw material intake pipeline and target product vent line are arranged in the hydrocarbon polymer water distilling apparatus; Heat exchanger on the raw material intake pipeline is installed in series; The raw material distillation of the stove that pump and heating raw are used and at least one grade that is connected in series with pipeline or several grades; Vaporizer that useful pipeline is connected in series in each grade and water cooler, and the evaporator tube road of each grade is connected with corresponding heat exchanger.
Novel is: water distilling apparatus also adds to have and is installed in target product interceptor(-ter) on the target product vent line, after heat exchanger, and vaporizer is made and the cyclone evaporator of extraneous vertical type cylinder body wall heat insulation, that have the electricity consumption heater heats.
Suitable is mounting temperature sensor at the entrance and exit place of each grade distillatory cyclone evaporator.
Best, each grade distillatory water cooler is made air-water heater.
The application's hydrocarbon material distillating method and device for carrying out said thereof are different from immediate similar method, and therefore, the application's scheme satisfies the requirement of one of invention patent mandate condition novelty.
Whether the application's technical scheme meets the creationary state of the art analysis of one of invention patent mandate condition, shows as follows.
Reach in the device of working on this basis at the hydrocarbon material distillating method that proposes; With in the past known not simultaneously, in order to separate into liquid and vapor capacity, use the cyclone evaporator that has the vertical type cylinder body wall; This wall is heated to cut boiling lower limit, is used for discharging target product.Liquid-vapor mixture is defined as such in the speed (being about 20m/s) of cyclone evaporator inlet and the velocity profile in the cyclone evaporator: rely on light oil and the borderline turbulent flow of heavy oil Steam area; Accompany or follow the light oil distillate that cyclone evaporator comes out, what take out of only is the steam of a small amount of heavy oil fraction.This effect with utilize vertical type cylinder body wall heating can also compensate to be in the same place because of the thermosteresis that causes in cyclone evaporator inlet steam work of expansion adds with the measure of dispelling the heat to environment; Can clearly be divided into cut to hydrocarbon material, obtain qualified target product.
Owing to can rely on steam gravity and malleation in the cyclone evaporator; Liquid phase can be freely flows to pipeline along the wall of cyclone evaporator; Heat exchanger and interceptor(-ter), so, fixedly liquid level of heavy oil fraction in cyclone evaporator, can not formed; This means that accumulation and tangible heavy oil fraction steam that heavy oil fraction steam can not take place get in the product of light oil distillate.This also helps and obtains qualified target product.
Each invention of application connects such degree each other, so that forms a unified inventive concept, because an invention is to be used for realizing another invention, so the monistic requirement of invention is satisfied in such one group of invention.
Description of drawings
With n figure explanation the present invention, Fig. 1 is the process flow sheet of hydrocarbon polymer water distilling apparatus; Fig. 2 is the section of whirlwind distiller; Fig. 3 is light oil and the velocity profile of heavy oil fraction steam in cyclone evaporator; Fig. 4 is the interface chart of cyclone evaporator and interceptor(-ter).
Embodiment
Hydrocarbon material water distilling apparatus (Fig. 1) comprising: with first, second, third grade of distillation of raw material that pipeline is connected in series, and the pipeline 4 of transferring raw material, the stove 6 that pump 5, heating raw are used, it is to be connected with first step distillation with pipeline.Heat exchanger 7,8,9 is installed in series on feed line line 4.In the distillation of the first step raw material cyclone evaporator 10 is arranged, water cooler 11 has cyclone evaporator 12 in the distillation of second stage raw material, and water cooler 13 has cyclone evaporator 14, water cooler 15 in the distillation of third stage raw material.Each grade distillatory cyclone evaporator 10,12,14 usefulness pipelines correspondingly with water cooler 11,13,15 are connected, heat exchanger 7,8,9 correspondingly connects with the first step, the second stage, third stage distillatory cyclone evaporator 10,12,14.On the target product vent line, at heat exchanger 7,8, after 9, interceptor(-ter) 16,17,18 has been installed, be used for collecting heavy oil, diesel oil and raw gasline respectively.A container 19 that is used for collecting the gasoline target product is arranged in the device.TP 20,21 has been installed, 22,23,24,25 and 26 in outlet and ingress at each grade distillatory cyclone evaporator.
Each grade distillatory cyclone evaporator (Fig. 2) is to be grouped into conical portion by cylindrical, includes shell 27, thermal insulation layer 28, electric heater 29, inlet connection 30, downstream end 31, the export pipeline 32 that vapour phase is used, the outlet 33 that liquid phase is used.In device, used the structure of classical cyclone evaporator, it shows input and takes over the well-balanced of geometrical dimension, cyclone evaporator cylindrical part diameter and length and conical portion length ratio.
Heat exchanger 7,8,9th, the recuperative heater and the water cooler of combination, water cooler 11; 13,15th, air-water heater, the cooling of steam is to realize with the Controllable Air stream of blower fan; What pump used is toothed gear pump, and stove is a tubular type, can use thermopair as TP.
Device carries out work as follows
Deliver to stove 6 heating to hydrocarbon material with pump 5; Be heated to head and heat up in a steamer (heavy oil) boiling lower limit temperature; For example to 360 ℃, the raw material that heats from stove 6 enters into first step distillatory cyclone evaporator 10, through heating the vertical type cylinder body walls with electric heater 29; Keep 360 ℃ of temperature, the liquid-vapor mixture that generates therein separates into liquid and vapor capacity.In order to separate liquid-vapor mixture, use cf-.For example, when speed 10m/s and radius 5cm, dispersive liquid-vapor mixture stream is delivered to curvilinear surface being heated in advance; Create gravity field artificially, for example 200 times surpass terrestrial gravitation, at this moment; Along with reducing of the surface that is separated; The fast cohesion of liquid has hindered the back suction of the hydrocarbon components in the vapour phase receives, and along the vertical type cylinder body wall of cyclone evaporator heating, the liquid phase of the raw material that is processed flows down with form of film.
Liquid phase in the cyclone evaporator 10 (heavy oil) enters into tubular heat exchange 7, and cooling is discharged to interceptor(-ter) 16 then.Vapour phase is cooled to second cut boiling lower limit temperature in water cooler 11, and for example 200 ℃, get into second stage distillatory cyclone evaporator, here liquid-vapor mixture is divided into liquid and vapor capacity.Liquid phase (diesel oil) enters into tubular heater exchhanger 8, and cooling is discharged to interceptor(-ter) 17 then.The gas phase of second stage distillatory cyclone evaporator 12 gets into water cooler 13, is cooled to the 3rd cut boiling lower limit temperature, and for example 170 ℃, enter into third stage distillatory cyclone evaporator 14 then, here liquid-vapor mixture is divided into liquid and vapor capacity.Liquid phase (raw gasline) enters into tubular heater exchhanger 9, and cooling is discharged to interceptor(-ter) 18 then.The vapour phase of cyclone evaporator 14 gets into water cooler 15, and afterwards, the gasoline of generation is discharged in the container 19.Cyclone evaporator 10; 12; The TP 20～26 in 14 imports and exit is used for controlling the power of cyclone evaporator vertical type cylinder body wall electric heater, and the TP indication in cyclone evaporator exit should conform to the TP indication of ingress.What the liquid phase that the whirlwind distiller comes out was leaned on to interceptor(-ter) mobile through heat exchanger is the gravity of hydrocarbon vapor and the effect of malleation.
Industrial application
Hydrocarbon material distillatory method that proposes and the device that moves on than the basis, can build one hydrocarbon material clearly separate into several cuts effectively, the device of small volume and obtain qualified product, comprise gasoline, and without rectifying tower.This just can reduce the material usage of oil-processing units widely, and it means reduces processing plant's construction cost, shortens the time of putting into operation, consequently improves the efficient of infusion of financial resources widely, when especially developing new oil oil field.When separating other liquid mixture (for example obtaining alcohol etc.), the method and apparatus of proposition can demonstrate no small effect.
Claims (8)
1. the hydrocarbon material distillating method comprises the distillation of n level, at first; Be heated to head to raw material and heat up in a steamer the boiling point lower limit, the liquid-vapor mixture of generation enters into the distillation level, separates into liquid and vapor capacity at each grade liquid-vapor mixture; Liquid phase is discharged as target product; And vapour phase is cooled to next cut boiling point lower limit, it is characterized in that: the separation of liquid and vapor capacity is to have in the cyclone evaporator of vertical type cylinder body wall to carry out in all grades distillation, at this moment; Will be the vertical wall heating of each cyclone evaporator, the wall of each grade cyclone evaporator is heated to the lower limit of the cut boiling point of this grade target product.
2. according to the method for claim 1; It is characterized in that: from the target product outlet position that cyclone evaporator comes out; Relative floor surface should be not less than the most probable position of target product in the interceptor(-ter), and the interceptor(-ter) product inlet should be lower than the minimum possible position of target product.
3. according to the method for claim 1, it is characterized in that: each cyclone evaporator vertical type cylinder body wall heating power is controlled to such an extent that make the temperature of cyclone evaporator ingress liquid-vapor mixture equal the temperature of its exit vapour phase.
4. according to the method for claim 1, it is characterized in that: the cooling of vapour phase is to realize through controlled airflow.
5. according to the method for claim 1, it is characterized in that: the quantity of the target product cut that obtains by boiling point equals n+1, and n is the quantity of cyclone evaporator.
6. hydrocarbon material water distilling apparatus; Comprise: the intake pipeline of raw material; The export pipeline of target product; Be installed in series heat exchanger on the raw material intake pipeline, the stove that pump and heating raw are used and at least one or several grades the raw material distillation that are connected in series with pipeline, each grade comprises cyclone evaporator and the water cooler that is connected in series with pipeline; And; Each grade cyclone evaporator is connected with corresponding heat exchanger with pipeline, it is characterized in that: it is installed in the interceptor(-ter) that the target product after heat exchanger is used on the target product vent line in addition, and cyclone evaporator is made with its external environment form of thermal insulation and the vertical type cylinder body wall of electricradiator heating is arranged.
7. according to the device of claim 6, it is characterized in that:, TP has been installed at the export and import place of each grade distillatory cyclone evaporator.
8. according to the device of claim 6, it is characterized in that: each grade distillatory water cooler is made the form of air-water heater.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| RU2006101935/04A RU2301250C1 (en) | 2006-01-24 | 2006-01-24 | Hydrocarbon feedstock distillation process and plant |
| RU2006101935 | 2006-01-24 | ||
| PCT/RU2006/000370 WO2007086774A1 (en) | 2006-01-24 | 2006-07-12 | Method for distilling a hydrocarbon material and a plant for carrying out said method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101360807A CN101360807A (en) | 2009-02-04 |
| CN101360807B true CN101360807B (en) | 2012-12-12 |
Family
ID=38309476
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200680051680.3A Expired - Fee Related CN101360807B (en) | 2006-01-24 | 2006-07-12 | Method for distilling a hydrocarbon material and a plant for carrying out the method |
Country Status (4)
| Country | Link |
|---|---|
| CN (1) | CN101360807B (en) |
| EA (1) | EA010729B1 (en) |
| RU (1) | RU2301250C1 (en) |
| WO (1) | WO2007086774A1 (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2458297C1 (en) * | 2011-03-10 | 2012-08-10 | Общество С Ограниченной Ответственностью "Аэрогаз" | Gas mixture separation method |
| RU2458298C1 (en) * | 2011-03-10 | 2012-08-10 | Общество С Ограниченной Ответственностью "Аэрогаз" | Gas mixture separation method |
| CN103768818B (en) * | 2012-10-24 | 2017-03-29 | 辽宁左旋节能科技有限公司 | Negative-pressure type hydrocarbon solvent distilling machinery |
| CN103436283B (en) * | 2013-09-12 | 2015-05-13 | 扬中市金元化工电力设备厂 | Distillation kettle |
| WO2015084205A1 (en) * | 2013-12-02 | 2015-06-11 | Игорь Иванович ГЛИНЯСТИКОВ | Hydrocarbon raw material distillation method |
| RU2607089C2 (en) * | 2013-12-18 | 2017-01-10 | Надежда Васильевна Копыл | Method of controlling process control and list of produced oil products during oil refining (versions) |
| RU2628508C1 (en) * | 2015-04-29 | 2017-08-17 | Надежда Васильевна Копыл | Processing method of heavy vacuum gasoil |
| RU2683267C1 (en) * | 2018-10-01 | 2019-03-27 | Александр Владимирович Данилов | Installation for processing liquid hydrocarbons |
| RU2701860C1 (en) | 2019-03-19 | 2019-10-02 | Общество с ограниченной ответственностью "Научно-производственное объединение ЭТН-Циклон" | Pyrolysis method of liquid and gaseous hydrocarbons and device for its implementation |
| CN118079420A (en) * | 2024-04-29 | 2024-05-28 | 安徽益沣石化有限公司 | Mixed carbon four raw materials purification device |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2043779C1 (en) * | 1994-02-28 | 1995-09-20 | Александр Васильевич Пушмынцев | Installation for refining of crude oil and oil products |
| RU2091432C1 (en) * | 1995-05-26 | 1997-09-27 | Научно-производственная фирма "Южуралнеруд" | Method of producing stable long fraction of light hydrocarbons from oil-gas condensate |
| RU2186085C2 (en) * | 1998-07-20 | 2002-07-27 | Общество с ограниченной ответственностью "Интербизнеспроект" | Method of producing motor fuels from hydrocarbon raw materials |
| RU2211853C2 (en) * | 2001-07-23 | 2003-09-10 | Общество с ограниченной ответственностью "Интербизнеспроект" | Atmospheric-and-vacuum distillation unit for producing fuel fractions from hydrocarbon feedstock |
-
2006
- 2006-01-24 RU RU2006101935/04A patent/RU2301250C1/en not_active IP Right Cessation
- 2006-07-12 EA EA200801088A patent/EA010729B1/en not_active IP Right Cessation
- 2006-07-12 WO PCT/RU2006/000370 patent/WO2007086774A1/en active Application Filing
- 2006-07-12 CN CN200680051680.3A patent/CN101360807B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2043779C1 (en) * | 1994-02-28 | 1995-09-20 | Александр Васильевич Пушмынцев | Installation for refining of crude oil and oil products |
| RU2091432C1 (en) * | 1995-05-26 | 1997-09-27 | Научно-производственная фирма "Южуралнеруд" | Method of producing stable long fraction of light hydrocarbons from oil-gas condensate |
| RU2186085C2 (en) * | 1998-07-20 | 2002-07-27 | Общество с ограниченной ответственностью "Интербизнеспроект" | Method of producing motor fuels from hydrocarbon raw materials |
| RU2211853C2 (en) * | 2001-07-23 | 2003-09-10 | Общество с ограниченной ответственностью "Интербизнеспроект" | Atmospheric-and-vacuum distillation unit for producing fuel fractions from hydrocarbon feedstock |
Also Published As
| Publication number | Publication date |
|---|---|
| RU2301250C1 (en) | 2007-06-20 |
| WO2007086774A1 (en) | 2007-08-02 |
| CN101360807A (en) | 2009-02-04 |
| EA010729B1 (en) | 2008-10-30 |
| EA200801088A1 (en) | 2008-08-29 |
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