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WO2009074837A1 - Production et fractionnement de brai et brai à point de ramollissement élevé - Google Patents

Production et fractionnement de brai et brai à point de ramollissement élevé Download PDF

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Publication number
WO2009074837A1
WO2009074837A1 PCT/IB2007/003836 IB2007003836W WO2009074837A1 WO 2009074837 A1 WO2009074837 A1 WO 2009074837A1 IB 2007003836 W IB2007003836 W IB 2007003836W WO 2009074837 A1 WO2009074837 A1 WO 2009074837A1
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WO
WIPO (PCT)
Prior art keywords
pitch
heating
softening point
product
molten metal
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/IB2007/003836
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English (en)
Inventor
Donald P. Malone
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
DTX Technologies LLC
Original Assignee
DTX Technologies LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by DTX Technologies LLC filed Critical DTX Technologies LLC
Priority to PCT/IB2007/003836 priority Critical patent/WO2009074837A1/fr
Publication of WO2009074837A1 publication Critical patent/WO2009074837A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C1/00—Working-up tar
    • C10C1/04—Working-up tar by distillation
    • C10C1/16—Winning of pitch
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C1/00—Working-up tar
    • C10C1/19—Working-up tar by thermal treatment not involving distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C3/00—Working-up pitch, asphalt, bitumen
    • C10C3/002—Working-up pitch, asphalt, bitumen by thermal means

Definitions

  • the invention relates to pitch production and fractionation, e.g., increasing the softening point of a crude pitch feed by removing distillable components and high softening point pitch products.
  • Wood tar has enjoyed a reputation as a sticky substance for over 100 years.
  • North Carolina has a semi-official nickname of "The Tar Heel State” and the term is now one of admiration, rather than fear.
  • the State Library of North Carolina reports the nickname relates to a civil war battle in which tenacious North Carolina fought on after troops from other rebel states left the field.
  • the North Carolina troops responded to requests, from the rebel troops, asking if there was any tar left in the state, answering that Jeff Davis had purchased all the tar in North Carolina.
  • Creecy relates that General Lee, upon hearing of the incident, said: “God leave the Tar Heel boys,” and from that they took the name (Adapted from Grandfather Tales of North Carolina by R.B. Creecy and Histories of North Carolina Regiments, Vol. Ill, by Walter Clark.
  • wood tar pitch was the primary pitch product for millennia, it gradually was displaced by pitch products derived from coal and, eventually, from petroleum.
  • pitch refining processes are similar whether the starting material is derived from wood, coal or petroleum.
  • vaporizable components are removed from non-vaporizable or non-distillable components (the pitch portion of the product).
  • the removal of progressively more of the distillable components from the pitch fraction increases the softening point of the remaining pitch.
  • wood tar pitch if too much turpentine is left in the pitch, the pitch is too soft.
  • coal tar pitch if too much creosote, or other solvent, remains in the pitch, the softening point is too low.
  • petroleum pitch as distillable hydrocarbons are removed, the softening point of the product pitch increases.
  • High softening point pitches for myriad reasons. These materials have a high coking value, an essential pitch property for making carbon containing artifacts and carbon fibers. High softening point pitch materials, and intermediate products containing them, have greater mechanical strength, both during manufacture and in the finished product, as compared to like products made from lower softening point pitch. Higher carbon contents, in pitch and in products made from pitch, usually mean higher strength and better product performance. High softening point pitch is mostly carbon, and pitch value is like that of other forms of carbon, diamonds are denser, and more valuable, than graphite.
  • pitch producers have sought higher softening point products.
  • Some refiners operate pitch fractionators under vacuum (to reduce the temperatures required to vaporize volatiles). Some use a wiped film evaporator, which relies on thin films and brute force mechanical wiping to prevent the sticky pitch from staying too long in contact with a hot metal wall.
  • Various combinations of all of the above approaches have been tried, as refiners tried to get around an upper limit on pitch softening point which had been set by their equipment and/or approach to pitch fractionation.
  • US 4,673,486 taught treating a solvent de-asphalted fraction with a carrier gas, and thermally cracking at 400 - 600 0 C to produce a gas oil fraction and a pitch product.
  • Ashland Petroleum obtained a series of patents on high softening point pitches, primarily for manufacture of carbon fiber.
  • US 4,671,864 taught vacuum flashing, or use of a wiped film evaporator (WFE), to reduce residence time of pitch at high temperature and form a pitch having a softening point of about 250 0 C.
  • WFE wiped film evaporator
  • US 5,238,672 taught heating isotropic pitch with inert gas, at high temperature, to make mesophase pitch.
  • US 5,316,654 taught use of WFE to make high softening point pitch.
  • US 5,429,739 taught use of a thin film, reduced pressure and partial oxidation to make high softening point pitch, converting a conventional pitch to high softening pitch in a WFE.
  • the Eureka ® Process developed by Kureha Chemical Industry Co. Ltd and Chiyoda, has been used for over 20 years to make pitch products.
  • the process injects steam into the pitch forming reactor to create a pseudo vacuum and keep the molten pitch as a homogeneous liquid.
  • the molten metal bath was very efficient at heating the pitch.
  • Molten metal was relatively free of hot or cold spots, because of its high thermal conductivity. Most important, crude pitch does not stick to molten metal, eliminating the sticking and coking problem associated with hot metal.
  • molten metal also permits a flexible design approach, permitting injection of the metal into the oil or vice versa, though not necessarily with equivalent results.
  • pitch or a pitch precursor
  • pitch producers have many more degrees of freedom to pursue the best pitch product, in a process which is fairly tolerant of mistakes. While mistakes may be made, they will not stick to the molten metal, so pitch formation or pitch fractionation can generally continue in operation even if some coke solids are produced by mistake.
  • the present invention provides a process for heating and fractionating a liquid hydrocarbon feed to produce a liquid pitch product having a softening point above 90 0 C comprising heating said liquid hydrocarbon feed by direct contact heat exchange with an immiscible molten fluid for a time sufficient to induce at least one of thermal polymerization and vaporization to produce heated crude pitch, vaporizing at least a portion of said heated crude pitch to produce a vapor phase and a liquid pitch product having a desired softening point and recovering said liquid pitch product phase as a product of the process.
  • the present invention provides a pitch product made by this process, preferably one having a softening point above 400 0 C.
  • FIGURE 1 is a simplified schematic drawing of a preferred embodiment wherein a low softening point pitch, or a pitch precursor, is heated in a single molten metal bath, with injection of feedstock into a lower portion of the molten metal bath, to produce a high softening point pitch.
  • Figure 2 is a block flow diagram of a multi-zone molten metal pitch process, analogous to a multi-tray fractionator.
  • a feedstock e.g., a crude pitch to be fractionated, or a pitch pre-cursor such as FCC slurry oil
  • a feed storage system 10
  • Preheated feed is charged via lines 14 and 20 through optional pump 28 into direct thermal exchange heating zone 30.
  • DTX will be used to refer to this zone or this approach, using molten metal for Direct Thermal eXchange (DTX). Any heat transfer fluid that is immiscible with, and preferably much denser than, the feed may be used, but molten metal is ideal. In the embodiment shown, molten metal circulates from the bottom to the top of contactor vessel 30.
  • DTX fluid is removed from the DTX heating zone 30 by line 36, heated in heater 38 to produce heated molten metal which is discharged via line 40 to heating zone 30.
  • Heater 38 may use electrical resistance elements, a fired heater, superheated steam or the like as a heat source. Although a separate molten metal heater 38 is shown, it is also possible to dispense with the separate molten metal heater and use electric resistance heaters or other heating jacket means, not shown, disposed around the heating zone 30 to satisfy the heat demand of the process. Heat transfer fluid flow through heater 38 may be controlled by natural convection, as shown, or a pump, not shown, may be used.
  • the total liquid level in the contactor, 14, is maintained by a vertical outlet pipe, 32, through which all gas, vapor and liquid leave the vessel and flow through line 34, to the separator vessel, 42.
  • the inventory of heat transfer fluid sets its level in the contactor or heater 30.
  • the level of the heat transfer fluid, 31, is relatively high as shown in Figure 1, the crude pitch feed is the predominately dispersed phase and the molten metal heat transfer fluid is the predominately continuous phase.
  • the molten metal phase 31 is continuous and fills the lower portion of vessel 30.
  • Preheated feed is charged to or near the bottom of the molten metal phase.
  • the entering crude pitch is rapidly heated by direct contact with molten metal. With heating, some of the vaporizable components of the feed are vaporized.
  • there are three phases in the molten metal bath 31 - the continuous metal phase a generally dispersed liquid phase of injected feed and a generally dispersed gas phase of bubbles formed by heating and vaporization of volatile components in the liquid feed.
  • the heated hydrocarbon liquid and vapor phases pass up through the continuous molten metal phase, with additional heating and vaporization occurring as the liquid pitch rises in the molten metal bath.
  • the liquid and vapor phases emerge from the molten metal continuous phase 31 and enter another continuous liquid phase 33, comprising heated pitch, through which bubbles of pitch vapor ascend.
  • a modest inventory of pitch liquid is maintained above the molten metal bath, with the lower limit on pitch liquid bed depth set by the top layer of the molten metal bath and the upper limit on pitch liquid set by vapor/liquid withdrawal means 32 disposed a distance above the molten metal bath.
  • Pitch liquid will accumulate in region 33 until the pitch liquid level is sufficiently high so that the net input of pitch liquid is removed or entrained with gas flow through outlet 32.
  • Heated pitch liquid and vapor components are then transferred via line 34 to vessel 42 wherein pitch vapor is allowed to separate from pitch liquid.
  • Pitch liquid with the desired softening point is withdrawn from vessel 42 via line 44 and collected in product tank 46.
  • the vapors produced by pitch fractionation are removed via line 48 and used as a heat exchange fluid to preheat incoming crude pitch in heat exchanger 50.
  • the cooled pitch vapors are withdrawn from exchanger 50 and charged via line 51 to fin fan cooler 52 or other heat recovery or cooling means, not shown, to produce a cooled and condensed pitch overhead vapor stream which is charged via line 53 to overhead receiver 54.
  • a pitch overhead receiver vapor phase is removed via line 60 and charged to product storage means 62, or burned as fuel by means not shown.
  • FIG. 2 is a simplified, block diagram of the process flow involved when two stages of molten metal heating of a crude pitch, or a pitch precursor, occur.
  • the process flow is somewhat similar to that which occurs in a fractionator with two trays, at least in terms of vapor and liquid flow, but very different in terms of temperature.
  • Molten metal flows down the "distillation column", while crude pitch feed is added via line 128 to the bottom of the column.
  • distillation stage 132 for further heating and vaporization.
  • the vapor phase from the first distillation stage may be removed from the process or passed up with the partially refined crude pitch into the second stage. Temperatures increase up the column, with the temperature highest in the top or second stage and lowest in the first stage. This temperature profile is achieved because the metal starts cooling as soon as it enters the "tower” via line 140 and starts work heating and vaporizing the crude pitch.
  • the metal enters the top of the "fractionator” at its peak temperature and is cooled by heating and vaporizing the pitch liquid and/or vapor removed via line 134 from the top distillation stage.
  • Molten metal is preferred and any metal can be used as part or all of the molten bath, so long as it is in a liquid phase at the desired operating temperature.
  • Metals which can be used include lead, tin, antimony, mercury, cadmium, sodium, potassium, bismuth, indium, zinc, gallium. Not all metals will give equal results and some present significant safety concerns, e.g., lead or mercury, but they can be included as part of the molten metal bath, if desired.
  • the invention contemplates the use of a range of molten metals for the high-intensity drying and/or heating process. These include low-melting point metal alloys. When simple drying or only a modest amount of thermal processing is desired, the candidate molten fluids may have melting points typically ranging from 60 - 23O 0 C or higher.
  • the heating fluid be immiscible with the liquid hydrocarbon feed and substantially denser.
  • the interfacial surface tension between the molten metal heat transfer media, or other molten fluid, and the liquid crude pitch feed should be sufficiently high to prevent sticking of the pitch to molten fluid.
  • the thermal conductivity of the molten fluid should be sufficiently high to ensure that the molten heating fluid remains in a liquid state during use, so that it does not solidify to form a solid film or freeze cone at the point of feed injection or contact.
  • the fluid conducts heat from the body of the molten bath to the interface contact region between drops or streams of feed and molten heating medium, or drops or streams of molten heating medium when the feed is the continuous phase.
  • molten metal alloys is preferred due to their high interfacial surface tension with both high softening point pitch product and trash that may be found in the feed. Metals are also preferred over other immiscible fluids due to their high thermal conductivity.
  • An additional benefit is the high density of molten metal relative to feed, which promotes rapid transit of one fluid through the other and plenty of motive force should baffles or column packing be used.
  • the Table summarizes melting points for several recommended molten metal eutectic alloy materials, when only moderate severity heating is required. This alloy information is taken from information reported in US 5,619,806, which is incorporated by reference.
  • the metallic material of the bath may consist of an alloy selected from the group that includes: Ga/In, Bi/In, In/Sn, Bi/Pb, Bi/Sn, Sn/Pb, Sn/Zn, and Sn/Cu.
  • molten metal temperatures can be used, from high to low. Based on the float bath process for making plate glass, tin has ideal properties when a relatively high temperature bath is desired. Tin has a melting point of 232°C and a boiling point of 2623°C. This means that a range of temperatures can be achieved in the molten metal bath, ranging from temperatures near the boiling point of water (when a low melting alloy like Wood's metal is used) to temperatures above
  • Feedstocks 500 0 C.
  • a tin-bismuth alloy is preferred.
  • any pitch feed containing volatile components can be heated using the process of the present invention.
  • the vaporizable components may include turpentine.
  • the vaporizable components may include creosote.
  • the vaporizable components may include normally liquid hydrocarbons, typically boiling in the gas oil or vacuum gas oil range.
  • a pitch fraction may also contain water or other diluents, either as contaminants or as a result of some mishap in blending or manufacture.
  • Any pitch precursor heretofore used to form pitch may be used, e.g., slurry oil, an aromatic rich heavy residual oil product of the fluidized catalytic cracking process. SOFTENING POINT v. PERCENT FRACTIONATION
  • the process of the present invention does the same thing as prior art pitch fractionation processes, i.e., feedstocks, % recovered as an overhead fraction, and response of the residue or pitch fraction in terms of softening point. What is profoundly different is the ease with which a significant amount of the volatile material can be removed from a pitch feed.
  • the process of the present invention also allows pitch producers or pitch refiners to operate in regions not attainable using prior art techniques.
  • the thermal reactor was a length of nominal 10 cm (4 inch schedule 40) stainless steel pipe.
  • the metal alloy used was a tin-bismuth eutectic that is 42% tin and 58% Bismuth.
  • the depth of molten metal was about 50 cm, with about 30 cm of freeboard or vapor space above the molten metal.
  • the stainless steel pipe was heated by a cylindrical heater, an electric jacket with a thermostat.
  • the initial series of tests on feed was conducted at about 316°C molten metal bed temperature.
  • the feed was fed into the bottom of the molten metal bath via a 6 mm nipple to which a length of 3 mm SS tubing was affixed.
  • the tubing did not extend into the molten metal bath.
  • the process ran under vacuum, estimated at about 3.5 - 7 kN/m 2 (0.5 - 1 psia), but the pressure gage used was not very accurate at these low pressures.
  • the preferred metal composition is the tin-bismuth eutectic that is 42% tin and 58% Bismuth.
  • the pitch feed has a significant amount of "light ends", or vaporizable contaminants, then it may be preferable to subject the pitch feed to a preliminary treatment, in either a conventional fractionator or a DTX heater, operating at lower temperature and less vacuum, atmospheric pressure, or even a positive pressure, to strip out the light ends, so that the vacuum system will not be overwhelmed with volatiles and the plant will run smoothly.
  • a preliminary treatment in either a conventional fractionator or a DTX heater, operating at lower temperature and less vacuum, atmospheric pressure, or even a positive pressure, to strip out the light ends, so that the vacuum system will not be overwhelmed with volatiles and the plant will run smoothly.
  • the DTX heater It is possible to operate the DTX heater at any temperature and pressure used in any of the prior art patents to produce pitch.
  • the temperature and pressure in the DTX heater are the same as those experienced in a prior art process, e.g., one using a WFE to remove volatile components from pitch, roughly the same products will be produced.
  • the DTX heater operates with ease in the operating conditions of the prior art, it is not constrained by these conditions, particularly as to temperature.
  • the DTX heater can operate at higher temperatures than was possible in the prior art, leading to new pitch products, with unusually high softening points. It is possible to use the DTX heater to make minor adjustments to product properties of a refined pitch.
  • a refiner with a large investment in a conventional pitch plant may use DTX heating as a pre- or post- treatment step.
  • An example of a pretreatment step is de-bottlenecking an existing facility by removing some light ends from the crude pitch feed, to increase capacity of a conventional plant.
  • a post-treatment step would to allow a pitch with a softening point of 107 0 C to be made using the conventional plant, with a modest portion of the conventional product given a mild DTX heating treatment to produce a pitch with a softening point of 135°C.
  • multiple DTX crude pitch treatments may be practiced, as when two, or more, DTX heaters successively contact a crude pitch stream.
  • DTX heater might dehydrate a crude pitch stream and/or remove light ends, materials boiling in the light naphtha range, e.g., pentane and lighter materials.
  • a second DTX heater could remove heavy naphtha and/or gas oil boiling range materials at atmospheric pressure, or under a slight vacuum, producing an intermediate pitch product with a softening point of 1 15 to 149°C.
  • this 149°C softening point is well above that achievable when conventional pitch fractionation is processed, but when a DTX heater is used, it is possible to run this second stage at sufficiently high temperature to drive off the amount of vaporizable hydrocarbons desired and produce a relatively high softening point pitch product, though some vacuum or steam injection will usually be required as temperatures increase to produce the higher softening point product. Any third, or subsequent, DTX heating stages will usually be run at a vacuum, so that a sufficient amount of volatile material can be removed without resorting to unduly high temperatures, though it should be recognized that the DTX heater and coking thereof will not be limiting factors, rather product degradation will be the limiting factor.
  • each stage is roughly equivalent to a single perfect fractionation stage.
  • pitch product is the most valued and/or the most important product, in that pitch product properties are not greatly sensitive to the molecular weight range of diluent present in pitch. If pitch properties are the only important factor, and the overhead's value is about the same whether it is a single pure stream or 2, 3 or more separate product streams, then it will be feasible to run using only a single, or just two, stages of DTX heating to achieve the desired pitch product.
  • Pitch refiners may wish to operate under a hard vacuum, mild vacuum, atmospheric or super-atmospheric pressure, to minimize vapor volumes and facilitate processing of streams with large amounts of water and/or volatile components. Higher pressures permit a more compact facility to be built.
  • molten metal usually a metal alloy
  • a heat range within that required for the desired process objectives.
  • simple dehydration is all that is required, and this will usually be a first or preliminary treatment rather than the entire process
  • molten metal which is molten in the 80°C + temperature range is suitable.
  • the metal must remain molten at temperatures above 100 0 C to say 600 0 C.
  • a heat range of 200 0 C to 700 0 C or higher may be desirable.
  • the upper limit on temperature/choice of the metal alloy is determined by volatility and process constraints.
  • the preferred molten metals will have a low vapor pressure at the temperatures used, so that loss of molten metal due to "dusting" or for any other reason is less than 1% a day.
  • the metals chosen should not be corrosive under process conditions and preferably are non-toxic, for safety.
  • each DTX heating stage may have about the same composition as overhead products obtained in the past using conventional heating methods, e.g., a WFE, to produce a given softening point pitch product.
  • the pitch products of DTX pitch fractionation can duplicate pitch products made using conventional technology.
  • the new manufacturing process allows production of higher softening point pitch products, with over an order of magnitude reduction in capital cost for the plant and a like reduction in operating costs, as compared to a process using WFE.
  • WFE was the best approach to making, e.g., 260 0 C softening point pitch, but such plants are expensive to build, costly to maintain and produce relatively small amounts of pitch.
  • attempts were made to improve the productivity of WFE by addition of oxygen to increase throughput, but such approaches only modestly increase production and oxygen can degrade the product and create safety concerns.
  • One of the advantages of the molten metal approach, especially as compared to oxygen addition, is that the molten metal does not do anything other than heat the pitch, there is no chemical reaction with any of the pitch feed or products.
  • the DTX approach is not restricted to a thin film of product. There is no need for mechanical wipers, the molten metal bath is inherently non-sticky and pitch passes through it, or vice versa, readily.
  • the DTX approach is inherently reliable, there need be no moving parts in the plant, except for external product addition or withdrawal. Refiners are used to working with hot fluids and much "off the shelf equipment is available to deal with working fluids at the temperatures and pressures contemplated for DTX fractionation of pitch. It is easy, by design, to have a DTX pitch fractionator as shown in Figure 1 with no mechanical moving parts in the plant.
  • Heat addition can be via the molten metal bath shown which uses the principal of a thermo-siphon reboiler to circulate molten metal, or an external heating jacket, can be used around the DTX heating vessel.
  • a DTX pitch former or fractionator is a molten metal heating bath, which can be built without any mechanical moving parts.
  • the DTX process uses thermodynamics, molten metal and fluid dynamics as an elegant solution to the problem of heating and vaporizing a crude pitch or pitch precursors to produce a higher softening point pitch. Such a process can run for years without shutdown.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Civil Engineering (AREA)
  • Structural Engineering (AREA)
  • Working-Up Tar And Pitch (AREA)

Abstract

L'invention porte sur un procédé de polymérisation thermique d'un précurseur de brai d'hydrocarbure liquide, ou de fractionnement d'un brai brut, par chauffage par contact direct avec un fluide fondu non miscible, de préférence un métal fondu. Un brai brut, qui peut contenir de l'eau, des contaminants et/ou des composants distillables, ou une charge d'hydrocarbure liquide telle qu'une huile boueuse de FCC, est chauffé par échange de chaleur par contact direct avec un fluide fondu, de préférence sur un bain de métal fondu, fonctionnant à une température de 100 à 6000°C. Le bain est maintenu à une température et une pression suffisantes pour induire une polymérisation thermique d'un précurseur de brai et/ou vaporiser une quantité désirée de contaminants ou de matière volatile à partir d'un brai brut pour produire un produit de brai ayant un point de ramollissement désiré. De nouvelles compositions de brai ayant un point de ramollissement élevé sont également produites.
PCT/IB2007/003836 2007-12-10 2007-12-10 Production et fractionnement de brai et brai à point de ramollissement élevé Ceased WO2009074837A1 (fr)

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WO2009074837A1 true WO2009074837A1 (fr) 2009-06-18

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017086985A1 (fr) 2015-11-20 2017-05-26 Stone, Richard Procédé et produit de brai en une seule étape

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Publication number Priority date Publication date Assignee Title
GB170617A (en) * 1920-05-26 1921-10-26 Thermal Ind & Chem Tic Res Co Improvements in stills for distilling tar, oils and the like
GB215095A (en) * 1923-02-02 1924-05-02 Thermal Ind & Chemical T I C R Improvements relating to the removal of matter from the surface of a liquid, particularly in working apparatus for heat treatment by means of molten metal
US1975433A (en) * 1932-03-23 1934-10-02 American Tar Products Company Process and apparatus for melting materials
GB573240A (en) * 1942-04-14 1945-11-13 Emil Hene Improvements in or relating to the heat treatment of petroleum and like hydrocarbon products and to the production therefrom of other products
GB966390A (en) * 1961-10-09 1964-08-12 Coal Tar Res Ass Thermal treatment of pitch
GB1106469A (en) * 1966-02-23 1968-03-20 Shell Int Research Process for the preparation of bitumens with a penetration index lower than - 1
EP0189150A2 (fr) * 1985-01-19 1986-07-30 Director-General of Agency of Industrial Science and Technology Procédé et dispositif pour la fabrication de fibres de carbone
US4673486A (en) * 1983-09-30 1987-06-16 Jushitsuyu Taisaku Gijutsu Kenkyu Kumiai Process for thermal cracking of residual oils

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB170617A (en) * 1920-05-26 1921-10-26 Thermal Ind & Chem Tic Res Co Improvements in stills for distilling tar, oils and the like
GB215095A (en) * 1923-02-02 1924-05-02 Thermal Ind & Chemical T I C R Improvements relating to the removal of matter from the surface of a liquid, particularly in working apparatus for heat treatment by means of molten metal
US1975433A (en) * 1932-03-23 1934-10-02 American Tar Products Company Process and apparatus for melting materials
GB573240A (en) * 1942-04-14 1945-11-13 Emil Hene Improvements in or relating to the heat treatment of petroleum and like hydrocarbon products and to the production therefrom of other products
GB966390A (en) * 1961-10-09 1964-08-12 Coal Tar Res Ass Thermal treatment of pitch
GB1106469A (en) * 1966-02-23 1968-03-20 Shell Int Research Process for the preparation of bitumens with a penetration index lower than - 1
US4673486A (en) * 1983-09-30 1987-06-16 Jushitsuyu Taisaku Gijutsu Kenkyu Kumiai Process for thermal cracking of residual oils
EP0189150A2 (fr) * 1985-01-19 1986-07-30 Director-General of Agency of Industrial Science and Technology Procédé et dispositif pour la fabrication de fibres de carbone

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017086985A1 (fr) 2015-11-20 2017-05-26 Stone, Richard Procédé et produit de brai en une seule étape
CN108291151A (zh) * 2015-11-20 2018-07-17 理查德·斯通 单级沥青工艺和产品
EP3377594A4 (fr) * 2015-11-20 2019-06-12 Stone, Richard Procédé et produit de brai en une seule étape

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