US20130240411A1 - Device and method for separating mixtures which contain oil or bitumen and additives - Google Patents

Device and method for separating mixtures which contain oil or bitumen and additives Download PDF

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Publication number
US20130240411A1
US20130240411A1 US13/813,251 US201113813251A US2013240411A1 US 20130240411 A1 US20130240411 A1 US 20130240411A1 US 201113813251 A US201113813251 A US 201113813251A US 2013240411 A1 US2013240411 A1 US 2013240411A1
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Prior art keywords
solvent
bitumen
oil
conduit
space
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US13/813,251
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English (en)
Inventor
Waldemar Karsten
Thomas Winter
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PHYSITRON GmbH
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PHYSITRON GmbH
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Publication of US20130240411A1 publication Critical patent/US20130240411A1/en
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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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
    • C10G1/045—Separation of insoluble materials
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/28—Recovery of used solvent
    • E—FIXED CONSTRUCTIONS
    • E01—CONSTRUCTION OF ROADS, RAILWAYS, OR BRIDGES
    • E01C—CONSTRUCTION OF, OR SURFACES FOR, ROADS, SPORTS GROUNDS, OR THE LIKE; MACHINES OR AUXILIARY TOOLS FOR CONSTRUCTION OR REPAIR
    • E01C19/00—Machines, tools or auxiliary devices for preparing or distributing paving materials, for working the placed materials, or for forming, consolidating, or finishing the paving
    • E01C19/02—Machines, tools or auxiliary devices for preparing or distributing paving materials, for working the placed materials, or for forming, consolidating, or finishing the paving for preparing the materials
    • E01C19/10—Apparatus or plants for premixing or precoating aggregate or fillers with non-hydraulic binders, e.g. with bitumen, with resins, i.e. producing mixtures or coating aggregates otherwise than by penetrating or surface dressing; Apparatus for premixing non-hydraulic mixtures prior to placing or for reconditioning salvaged non-hydraulic compositions
    • E01C19/1004—Reconditioning or reprocessing bituminous mixtures, e.g. salvaged paving, fresh patching mixtures grown unserviceable; Recycling salvaged bituminous mixtures; Apparatus for the in-plant recycling thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/02—Settling tanks with single outlets for the separated liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2221/00—Applications of separation devices
    • B01D2221/04—Separation devices for treating liquids from earth drilling, mining
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/44—Solvents
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/80—Additives

Definitions

  • the present invention relates to a device and to a method for separating mixtures which contain oil or bitumen and additives.
  • the device and the method are particularly applicable to separating stone chippings and bitumen in evacuated asphalt road surfaces.
  • the mineral phase can be separated from the oil phase also with oil sands and oil shale, and a separation of bitumen and carrier felt can be induced with the recycling of bitumen felt, oil binder and oil.
  • a method is disclosed in DE 600 10 533 T2,with which the aggregate is separated from the bitumen share, by way of a thermal decomposition of the bitumen encasing. Bitumen is thereby used as a fuel and is activated by introducing hot gases into a drum which contains the excavated material.
  • the method however has the disadvantage that it is coupled to the manufacture of new asphalt and may only be carried out at a high energy expense.
  • a device for separating mixtures, which contain oil or bitumen and additives, includes a reaction vessel, into which the mixture and a solvent can be brought through a feed opening and/or a filling conduit, into a reaction space, further including a supply container with a vapor space, at least one capture container with a withdrawal conduit and with a riser conduit, and a condensation vessel.
  • the mixture is filled in through the feed opening while the solvent is introduced through the filling conduit, but also only one opening can be provided for this purpose for space-saving reasons.
  • the opening in any case is closed via a valve.
  • the solvent dissolves the oil-containing or bitumen-containing material from the additives, in the reaction space in an initial method step.
  • the solvent dissolves the oil-containing or bitumen-containing material from the additives, in the reaction space in an initial method step.
  • the solvent laden with oil or bitumen in a further method step, is removed from the reaction space, while the additives remain in this. Thereafter, the material remaining in the reaction space is removed from this by way of a lock.
  • a transport belt below the lock said transport belt immediately transporting away the additives.
  • the material can be removed again through the feed opening, also by way of tilting the reaction vessel.
  • the oil-laden or bitumen-laden solvent from the reaction space collects in the supply container as a sediment on a base, while the solvent in the upper part of the supply container, the vapor space, is located in the gas phase.
  • At least one conduit, the withdrawal conduit departs from the base of the supply container, to capture containers. If the withdrawal conduit is opened, for example by way of opening a valve contained therein, then the oil-laden or bitumen-laden solvent flows into the capture container.
  • the capture container is heated in a further method step, in order to separate the solvent from the oil or bitumen.
  • the evaporated solvent is transported away via the riser conduit which leads from the capture container into the vapor space of the supply vessel, while the oil or bitumen stays back in the capture container.
  • a filled capture container can be removed after closure of the valves, and be replaced by an empty one.
  • the solvent is constantly kept in the vapor phase in the vapor space by way of a suitable temperature. Solvent can be supplied to the supply container through the riser conduit in a simple manner, without requiring separate pumps or other energy-consuming apparatus.
  • the vapor space is connected to the reaction space which in turn is in connection with the condensation vessel.
  • the solvent in one method step gets into the condensation vessel and is liquefied there.
  • the liquefied solvent from here can either be filled into a reaction vessel again, in order to start a renewed washing procedure.
  • the device according to the invention thus has the advantage of a significantly simpler construction compared to devices for separating stone chippings and bitumen, which are known from the state of the art.
  • a device according to the invention requires no wash drum and achieves a reliable separation of oil or bitumen and additives, even without the support of ultrasound.
  • the energy consumption for carrying out the method is significantly reduced compared to methods and devices known from the state of the art.
  • the reaction space at the discharge conduit includes a particle filter which prevents fine particles being sucked as well.
  • Mixing devices such as stirrers or ultrasound cleaning devices for the improved through-mixing of the solvent can also be contained in the reaction space, for supporting the washing procedure.
  • a device may advantageously include several reaction spaces which are connected parallel to one another. A washing procedure then takes place in each reaction space, wherein the individual washing procedures particularly advantageously take place in staggered manner with regard to time, in order to ensure a uniform accumulation of the separated materials.
  • Several capture containers can just as well be provided, in order to continuously capture oil or bitumen.
  • reaction space including a discharge conduit which is connected to the supply container.
  • discharge conduit can be connected to the vapor space.
  • a direct connection between the reaction space and the supply container is given by the discharge conduit, and this connection permits substances to be transported in a defined direction between the connected spaces.
  • the discharge conduit out of the reaction space into the supply container is advantageously designed according to the principle of a siphon. Thus a discharge is effected alone on account of the rising solvent level.
  • the vapor space can be connected via a conduit to the condensation vessel.
  • the solvent can be led directly out of the vapor space into the condensation vessel, condense more rapidly by way of this and also be brought more rapidly to the mixture for cleaning.
  • condensation vessel being in connection with the reaction space via a further conduit.
  • This has the advantage of a direct introduction of the condensed solvent into the reaction space, by which means the solvent can be brought onto the mixture to be cleaned or purified, in a more rapid manner.
  • the device according to the invention by way of a pump, can be maintained at a slight vacuum, thus e.g. between 5 mbar and 10 mbar below the atmospheric pressure.
  • a slight vacuum thus e.g. between 5 mbar and 10 mbar below the atmospheric pressure.
  • the pump or the blower which is used for this can be provided with an additional condenser which is cooled by a cooling device at a few degrees above 0° C. and condenses solvent vapors out of the discharge air, so that the solvent can be constantly reused and no exit of the solvent into the environment takes place.
  • the vapor space by way of a heater can be kept at a temperature of 60° C. to 65° C., in order to maintain the solvent in the vapor space in the vapor phase, since a boiling delay occurs at greater temperatures.
  • the capture container is advantageously held at a temperature of between 75° C. and 95° C. by way of a heating element for heating, but this range can be varied depending on the boiling point of the used solvent.
  • the condensation vessel can be held at lower temperatures, such as between 10° C. and 15° C., for condensing the solvent and this can be effected by way of a cooling element. With the application of greater temperatures, a larger condensation vessel is required, whereas lower temperatures lead to an increasing condensation of water which again must be removed through a filter.
  • a further embodiment can envisage the reaction space including a conveying device, on which the mixture containing oil and bitumen and additives, and the solvent are conveyed.
  • the mixture for this is led in a counter-flow to the solvent, by which means a particularly efficient washing by the solvent takes place.
  • the solvent is dichloromethane.
  • chloroform, diesel, naphtha, acetone, methanol, tetrahydrofurane, butyl methyl ether, carbon tetrachloride, propane gas, benzene or toluene can be applied for this purpose.
  • the separation of the oil-laden or bitumen-laden solvent from the additives in the reaction space can be controlled or regulated with regard to time, in order to increase the efficiency of the method.
  • a clouding of the solvent determined by a measurement apparatus which carries out a turbidity measurement, can be used as a control variable or controlled variable.
  • One advantageous further development can envisage a heating of the reaction space being carried out for drying the additives of the mixture and for removing the remaining solvent.
  • the method becomes more efficient on account of this, since the additives can be removed in a completely dried manner, and the removed solvent can be used for the renewed washing
  • reaction space for heating being heated about 10 minutes at a temperature of 60° C.
  • the reaction space can be heated for a shorter time at a temperature of over 100° C. in dependence on the applied material and the boiling point of the solvent, in order to shorten the drying times.
  • the air can be sucked through the reaction space, which is particularly advantageous if the device is maintained at a vacuum.
  • the device and the method are applied with the treatment of asphalt containing bitumen.
  • the end product of the method consists of bitumen or oil and additives, preferably mineral aggregates, and which were separated from one another by the method.
  • Embodiment examples of the method are represented in sketched manner in FIGS. 1 to 6 and are explained by way of these figures.
  • FIG. 1 is a schematic view of a first embodiment example of a device according to the invention, with several reaction vessels, wherein different steps of the method are represented in the individual reaction vessels,
  • FIG. 2 is an enlarged schematic view of one of the reaction vessels with a solvent feed conduit which is designed differently compared to the embodiment represented in FIG. 1 ,
  • FIG. 3 is a schematic view of a second embodiment example of a device according to the invention, with a single reaction vessel, in which a conveyor belt runs,
  • FIG. 4 is a representation corresponding to FIG. 3 with an embodiment example of an alternative solvent feed onto the conveyor belt,
  • FIG. 5 is a representation according to FIG. 3 , with a worm instead of the conveyor belt and
  • FIG. 6 is a representation of the device, according to FIG. 5 , with the worm and the solvent feed through the worm.
  • FIG. 1 shows a schematic view of a device according to the invention, with several reaction vessels, wherein different steps of the method are represented in the individual reaction vessels.
  • reaction vessels 1 - 8 are each constructed identically, even if for reasons of an improved overview, not all components are represented on each reaction vessel 1 - 8 .
  • Each reaction vessel 1 - 8 includes a reaction space 11 which via a feed opening 12 and a valve contained therein, can be filled with the material 14 to be purified.
  • the material 14 to be purified in the present case is asphalt which contains bitumen or mineral additives.
  • liquid solvent 210 in the present case dichloromethane, can be filled into the reaction space 11 via a filling conduit 19 by opening the valve 18 contained therein.
  • the solvent 210 dissolves the oil-containing or bitumen-containing constituents of the material 14 to be purified, from the additives, which is hereinafter indicated as the “washing procedure”. Finally, the oil-laden or bitumen-laden solvent 210 , by way of the rising liquid level of the solvent 210 , is removed via a discharge conduit 16 in a bend 20 , out of the reaction space 11 and led into a supply container 100 .
  • This discharge conduit 16 in the present embodiment example is a siphon and can be closed via a valve 17 .
  • This washing procedure can be repeated until the desired degree of purity of the material 14 to be cleaned has been achieved. Also a simultaneous separation of several products can be effected by way of the provision of several supply containers.
  • a mixing device 300 which includes a stirrer or an ultrasound cleaning device is attached for improving the mixing.
  • a measurement apparatus 310 which measures the clouding of the oil-laden or bitumen-laden solvent 210 and which controls or regulates the washing procedure in dependence on the measured clouding, is contained in the discharge conduit 16 . Thus additional solvent 210 is filled when the ascertained clouding is too high.
  • the measurement apparatus 310 for this purpose contains a light source, for example an LED, and a detector, e.g. a bolometer and measures the absorption of the light emitted by the light source, in the laden solvent 210 . Alternatively, another radiation source with a detector which matches this is also possible.
  • a particle filter 320 is contained in the reaction space 11 , below the bend 20 on the discharge conduit 16 , and this filter prevents fine particles being sucked as well.
  • This particle filter 320 is attached on a funnel-like widening which acts as a suction opening.
  • the reaction vessel is heated for about 10 minutes long to 60° C. or is heated for a shorter time to above 100° C., in order to dry the material 21 which has now been purified and to finally remove the remaining solvent residues. Air can also be sucked through the reaction space 11 for supporting the drying.
  • the material 21 which is now dried and purified is removed from the reaction space 11 via a lock 13 by way of opening a valve contained therein and can be transported further via a transport belt 15 .
  • the reaction vessels 1 - 8 represented in FIG. 1 are connected in parallel and permit a continuous purification of the material 14 to be purified.
  • the material 14 to be purified is filled into the reaction vessel 1 , whereas the material 14 has already been filled in the reaction vessel 2 and solvent 210 is now added.
  • the oil or bitumen is dissolved in the solvent 210 and flows via the discharge conduit 16 into the supply container 100 , and the same procedure is represented in the reaction vessel 4 , but here the clouding of the solvent 210 is already significantly reduced, since a large part of the oil or bitumen has already been washed out.
  • reaction vessel 5 a more extensive washing out of the solvent 210 is shown in the reaction vessel 5 , and this is represented by way of a constantly reducing clouding of the laden solvent 210 .
  • the solvent is removed from the reaction space 11 in the reaction vessel 6 and only the purified material 21 remains therein.
  • This vessel is therefore heated for drying the purified material 21 and for removing remaining solvent residues.
  • a heater is applied on the outer walls of the reaction vessel for heating, for this.
  • the lock 13 is opened by way of opening the valve and the purified material 21 falls onto a transport belt 15 running below the exit of the lock 13 .
  • new material 14 to be purified is filled into the reaction vessel 8 .
  • the washing procedure in the reaction vessels 1 - 8 is carried out at room temperature.
  • the solvent laden with oil or bitumen in the supply vessel 100 forms a sediment 110 which collects on the base of the supply vessel 100 . From there, this solvent sediment 110 via the opening of a valve 102 of a withdrawal conduit 101 gets into a capture container 103 , for example a barrel.
  • the capture container 103 is heated to a temperature of 75° C. to 95° C., so that the solvent 210 evaporates and the bitumen or the oil remains in the capture container 103 .
  • the vaporization can be accelerated by way of sucking or blowing air through the capture container.
  • the selected temperature range is designed for the use of dichloromethane as a solvent 210 and can slightly change with the application of different materials.
  • the vaporized solvent 210 escapes via a riser conduit 104 on opening the valve 105 contained in the riser conduit 104 , into a vapor space 120 .
  • This vapor space 120 in the supply container 100 is located above the sediment 110 and can be separated from this by way of separation elements.
  • a temperature of 60° C. to 65° C. and which is produced by a heater prevails in the vapor space 120 .
  • This temperature region maintains the solvent 210 in the gas phase while a boiling delay occurring at even higher temperatures is prevented.
  • the capture container 103 can be removed after heating and cooling the bitumen or oil and be replaced with a new one, wherein a continuous separation of bitumen or oil and a continuous exchange of the capture container 103 are made possible by way of the provision of several capture containers 103 .
  • the supply vessel 100 more specifically the vapor space 120 is connected to a condensation vessel 200 via a conduit 130 .
  • the gaseous solvent 210 via this conduit 130 gets into a condenser or a condensation vessel 200 which is maintained at a temperature of 10° C. to 15° C. by way of a cooling device. An increasing condensation of water occurs below these temperatures, and this water must be removed through a filter which is not represented.
  • the solvent 210 is liquefied in the condensation vessel 200 by way of condensation and can be fed again to the respective reaction vessels 1 - 8 via a filling conduit 19 .
  • the device is maintained at a slight vacuum, approx. 5 mbar to 10 mbar below atmospheric pressure, by way of a blower 190 or a pump. Due to this, it is impossible for solvent to exit into the surroundings on account of possibly present or occurring leakages.
  • the through-blowing of the capture container 103 and of the reaction spaces 11 is made possible by way of the blower 190 and the vacuum which is created by way of this.
  • This blower 190 is connected to an additional condensation vessel or condenser 180 which condenses solvent vapors out of the discharge air, so that the solvent is available for further washing procedure without an losses. For this, the condenser 180 is cooled down to a few degrees above 0° C.
  • reaction vessel 1 by way of example the reaction vessel 1 , is represented in an enlarged manner in FIG. 2 .
  • identical elements are provided with identical reference numerals.
  • the reaction vessel 1 now has no introduction of the solvent 210 effected from above into the reaction space 11 , but the solvent 210 coming from the condensation vessel 200 lying above the reaction vessel 1 is led through the filling conduit 19 firstly past the reaction vessel 1 .
  • the filling conduit 19 at its end includes a bend and runs out in a lower part of the reaction vessel 1 .
  • the filling conduit 19 includes a pump 23 for supporting a feed of solvent.
  • the solvent 210 however can also get into the reaction space 1 also without the application of the pump 23 due to the position of the reaction space 1 below the condensation vessel 200 .
  • An upwardly directed distributor head 22 which is formed in a hemispherical manner and includes openings on its surface, is attached at the end of the filling conduit 19 in the reaction vessel 1 , so that the solvent 210 can exit as uniformly as possible through the distributor head 22 and thus encompasses the material 14 to be purified.
  • FIG. 3 in a schematic representation shows a further embodiment example of a device for carrying out the method according to the invention.
  • the material 14 to be purified in the represented embodiment example oil sand which contains bitumen and mineral additives, is introduced into a reaction space 11 via a feed opening 12 .
  • the material 14 to be cleaned is introduced into a first receiver container 260 and from there is led via a valve into a second receiver container 270 which is opened or closed by way of the feed opening 12 .
  • the reaction space 11 includes a conveyor belt 220 as a conveying device, onto which, when the feed opening 12 is opened, the material 14 to be purified falls and is transported by the conveyor belt 220 in the direction of the condensation vessel 200 .
  • the conveyor belt 220 includes a multitude of capture grids 240 at uniform distances, on which the material 14 to be purified clings and is caught, for simplified transport.
  • the solvent 210 in the present case acetone, as a condensate, is deposited through a discharge conduit out of the condensation vessel 200 onto the conveyor belt 200 , at an end of the conveyor belt 220 which is opposite to the feed opening.
  • This discharge conduit for example can include a pipe conduit or a funnel system.
  • the conveyor belt 220 starting from the end, at which the material 14 to be purified is deposited, runs in a rising manner up to the end, at which the solvent 210 is deposited, so that the solvent 210 flows counter to the transport direction of the conveyor belt 220 .
  • the solvent 210 rinses through the material 14 to be purified in the counter-flow direction and dissolves the oil-containing or bitumen-containing constituents of the material 14 to be purified, from the additives, within the framework of the washing procedure.
  • the capture grids 240 can be simply passed by the liquid solvent 210 , while the solid constituents of the material 14 to be purified remain in the capture grids 240 and are transported.
  • the reaction space 11 hereby is maintained at a temperature in the range of 15° C. to 25° C.
  • the reaction space 11 is maintained at a temperature in the range of 17° C. to 23° C. In some embodiments, the reaction space 11 is maintained at a temperature of 20° C., thus room temperature. This can be effected by way of heating elements or cooling elements which are not shown in FIG. 3 for reasons of a better overview.
  • the sold constituents of the material 14 to be purified are thus purified or cleaned to an increasing extent and fall at the end of the conveyor belt 220 located below a condensation vessel 200 , from which the solvent 210 is brought onto the conveying belt 220 , into a capture device 280 provided with a heater 230 .
  • the capture device 280 is heated, for example about 10 minutes to a temperature of 60° C., in order to remove solvent residues remaining on the solid constituents.
  • the purified material 21 is removed out of the device through a lock 13 and can be used again, or should the purification not have been effected to a satisfactory extent, is deposited onto the conveyor belt 220 again and the washing procedure is carried out once again.
  • the solvent 210 which is conveyed into the gaseous condition by way of the heating of the heater 230 is fed via a further riser conduit 290 to the condensation vessel 200 where it condenses and is deposited afresh onto the conveyor belt 220 .
  • the further riser conduit 290 for this can be opened and closed via a valve 390 .
  • Conduits are pipe conduits in the embodiment examples represented in the figures.
  • the supply container 100 is located directly below the feed opening 12 and is in connection with the reaction space 11 .
  • the reaction space 11 includes a particle filter 320 below the end of the conveyor belt 220 which is situated below the feed opening 12 , in order to ensure that no solid constituents of the material 14 to be purified get into the supply container 100 .
  • the solvent 210 forms a solvent sediment 110 at the base of the supply container 100 .
  • a vapor space 120 is located above the sediment 110 .
  • the solvent 210 in the vapor space 120 is kept in the gaseous state by way of a heater 250 running around the supply container 100 , at a temperature of 60° C. to 65° C.
  • the base of the supply container 100 is closed by a valve 102 of a withdrawal conduit 101 .
  • the withdrawal conduit 101 connects the supply container 100 to a capture container 103 .
  • the valve 102 When the valve 102 is open, the solvent 210 can get through the withdrawal conduit 101 into the capture container 103 .
  • This capture container 103 is connected via a further valve to a barrel, but in an embodiment which is not represented, the capture container 103 may directly be a barrel and thus be separated from the device according to the invention and transported away, in a particularly simple manner.
  • the capture container 103 is heated by the heater 250 to 60° C. so that solvent 210 thus acetone evaporates and the bitumen or the oil remains in the capture container 103 . Air can be blown through the capture container 103 by way of a blower which is not shown, for accelerating the vaporization.
  • Vaporized solvent 210 escapes via a riser conduit 104 on opening the valve 105 contained in the riser conduit 104 , into the vapor space 120 . Since the reaction space 11 and the vapor space 120 are connected to one another, the vaporous solvent 210 can also get into the reaction space 11 , condense there and settle again on the conveyor belt 220 . The solvent vapor condenses at the latest on reaching the condensation vessel 200 , and the solvent 210 settles on the conveyor belt 220 in the liquid state.
  • the connection between the vapor space 120 and condensation vessel 200 in the represented embodiment example is effected via the reaction space 11 through the space above and below the conveyor belt 220 , but can also be designed as a separate conduit.
  • the condensation vessel 200 is kept at a temperature of 10° C. to 15° C. by way of a cooling device.
  • a blower 190 attached on the condensation vessel 200 maintains the device at a slight vacuum, thus roughly 5 mbar to 10 mbar below the atmospheric pressure. By way of this, an exit of solvent by way of leaks is avoided.
  • the blower 190 is connected to an additional condenser 180 and this condenser condenses the solvent vapors out of the discharge air, for which it is cooled to a few degrees above 0° C., and 3° C. in the represented embodiment example.
  • a condensation vessel 200 can be all devices together.
  • FIG. 4 in a schematic view corresponding to FIG. 3 represents a further embodiment example of the device for separating mixtures with a conveyor belt 220 .
  • the solvent 210 coming from the condensation vessel 200 in the embodiment example shown in FIG. 4 is collected in a capture space 330 at the lower end of the condensation vessel 200 and in contrast to the embodiment example shown in FIG. 3 can no longer get into the reaction space 11 in an uninhibited manner.
  • the capture space 330 includes a run-over protection 340 so that given a filled level of the solvent 210 in the capture space 330 , said level rising above the run-over protection 340 , the solvent 210 can run off into the reaction space 11 onto the conveyor belt 220 without intervention of a user.
  • the solvent 210 collected in the capture space 330 is pumped via a pump 23 into the reaction space 11 .
  • an end-pipe 340 with openings in the reaction space 11 is attached between a lower end and an upper end of the conveyor belt 220 .
  • the openings are located on the upper side of the end-pipe 340 , i.e. on a side which faces the material 14 to be purified.
  • the solvent enters into the reaction space 11 through the openings of the end-pipe 340 .
  • the solvent 230 in the end-pipe 340 is under pressure due to the pump 23 , so that the solvent 210 can be injected or sprayed out of the openings onto the conveyor belt 220 .
  • FIG. 5 A view of a device for separating mixtures with a worm 350 running in the reaction space instead of the conveyor belt 220 is shown in FIG. 5 , in a manner corresponding to FIG. 3 .
  • the worm 350 is driven by a drive unit 360 and rotates about a longitudinal axis.
  • the worm 350 functions similarly to an Archimedean screw, i.e. the material 14 to be purified is deposited onto the worm 350 via the feed opening 12 and is transported further in the direction of the capture device 280 by a worm thread 400 .
  • the solvent 210 flows through the material 14 to be purified, in a counter-flow and can be deposited directly from the condensation vessel 200 onto the worm 350 .
  • the condensation vessel 200 moreover yet includes a conduit 370 which departing from the condensation vessel 200 ends with the end-pipe 340 at the worm 350 .
  • the end-pipe 340 includes openings, through which the solvent 210 is sprayed onto the worm 350 .
  • the pump 23 is attached on the conduit 370 and sucks the solvent 210 out of the condensation vessel 200 and pumps it through the conduit 370 up to the end-pipe 340 .
  • FIG. 6 in a view corresponding to FIG. 5 represents a further embodiment example of the device for separating mixtures.
  • the conveying device is the worm 350 which is set into rotation about its longitudinal axis by the drive unit 360 and thus transports the material to be purified on the worm gear 400 .
  • the conduit 370 from the condensation vessel 200 into the reaction space 11 is however led through the drive unit 360 into an interior of the worm shaft 380 .
  • the worm shaft 380 includes openings extending in the direction of the rotation axis.
  • the solvent 210 exits through these openings into the reaction space 11 , wherein it is accelerated by the centrifugal force acting by way of the rotation of the worm 350 , through the openings of the worm shaft 380 and flows in a counter-flow through the material 14 to be purified.
  • One aspect of the invention includes a device for separating mixtures 14 which contain oil or bitumen and additives, wherein the device includes at least one reaction vessel 1 having a reaction space 11 , a feed opening 12 and a discharge conduit 16 , further including a supply container 100 having a vapor space 120 , further including at least one capture container 103 having a withdrawal conduit 101 and a riser conduit 104 , and further including a condensation vessel 200 , wherein the discharge conduit 16 is in connection with the supply container 100 , the supply container 100 via the withdrawal conduit 101 with the capture container 103 , the capture container 103 via the riser conduit 104 with the vapor space 120 , the vapor space 120 via a conduit 130 with the condensation vessel 200 , and the condensation vessel 200 via a further conduit 19 with the reaction space 11 .
  • a further aspect relates to a device according to the preceding aspect, wherein the reaction space 11 contains a particle filter 320 .
  • a further aspect relates to a device according to one of the preceding aspects, wherein stirrers or ultrasound cleaning devices 300 for improved mixing of a solvent 210 are contained in the reaction space 11 .
  • a further aspect relates to a device according to one of the preceding aspects, wherein several reaction vessels 1 , 2 , 3 , 4 , 5 , 6 , 7 , 8 , are arranged in parallel.
  • a further aspect relates to a device according to one of the preceding aspects, wherein the discharge conduit 16 includes a siphon.
  • a further aspect relates to a device according to one of the preceding aspects, wherein the device has a slight vacuum of 5 to 10 mbar below atmospheric pressure.
  • a further aspect relates to a device according to one of the preceding aspects, wherein the vapor space 120 has a temperature of 60° C. to maximal 65° C.
  • a further aspect relates to a device according to one of the preceding aspects, wherein the capture container 103 has a temperature of 75° C. to 95° C.
  • a further aspect relates to a device according to one of the preceding aspects, wherein the condenser 200 has a temperature of 10° C. to 15° C.
  • One aspect of the invention relates to a method for separating mixtures 14 which contain oil or bitumen and additives, having the following steps:
  • a further aspect of the invention relates to a method according to the preceding aspect, wherein the solvent 210 includes dichloromethane, chloroform, diesel, naphtha, acetone, methanol, tetrahydrofurane, butyl methyl ether, carbon tetrachloride, propane gas, benzene or toluene.
  • the solvent 210 includes dichloromethane, chloroform, diesel, naphtha, acetone, methanol, tetrahydrofurane, butyl methyl ether, carbon tetrachloride, propane gas, benzene or toluene.
  • a further aspect relates to a method according to one of the preceding aspects, wherein the separation of the oil-laden or bitumen-laden solvent 210 is controlled or regulated in a temporal manner, preferably via a turbidity measurement of the solvent 210 .
  • a further aspect relates to a method according to one of the preceding claims, wherein the reaction space 11 is heated for 10 minutes to 60° C. for heating.
  • a further aspect relates to a method according to one of the preceding aspects, wherein air is sucked or blown through the capture container 103 , for the accelerated vaporization of the solvent 210 .
  • a further aspect relates to a method according to one of the preceding aspects, wherein bitumen-containing asphalt is used as a mixture 14 .

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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)
  • Architecture (AREA)
  • Civil Engineering (AREA)
  • Structural Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
US13/813,251 2010-07-30 2011-07-29 Device and method for separating mixtures which contain oil or bitumen and additives Abandoned US20130240411A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP10075333A EP2412783A1 (de) 2010-07-30 2010-07-30 Vorrichtung und Verfahren zum Trennen von Gemischen, welche Öl oder Bitumen und Zusatzstoffe enthalten
EP10075333.4 2010-07-30
PCT/EP2011/003866 WO2012013363A1 (de) 2010-07-30 2011-07-29 Vorrichtung und verfahren zum trennen von gemischen, welche öl oder bitumen und zusatzstoffe enthalten

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US20130240411A1 true US20130240411A1 (en) 2013-09-19

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US (1) US20130240411A1 (de)
EP (1) EP2412783A1 (de)
CN (1) CN103314077A (de)
CA (1) CA2806748A1 (de)
DE (1) DE112011102547A5 (de)
WO (1) WO2012013363A1 (de)

Cited By (5)

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WO2018125952A1 (en) * 2016-12-30 2018-07-05 Stojan Kotefski Methods for reclaiming or recycling asphalt and asphalt and asphalt components produced thereby
US10640712B2 (en) 2016-11-18 2020-05-05 Stojan Kotefski Methods for retrieving, reclaiming, or recycling petroleum-based products and byproducts
CN112057884A (zh) * 2020-07-22 2020-12-11 江苏高速公路工程养护技术有限公司 一种沥青分子测试用流动液循环使用处理方法及系统
US11549016B2 (en) 2016-11-18 2023-01-10 Stojan Kotefski Hybrid crude oil and methods of making the same using petroleum-based waste stream products
WO2024084358A1 (en) * 2022-10-19 2024-04-25 Russell Atlas James System, method, and apparatus for recycling asphalt shingles

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CN108181196A (zh) * 2017-11-22 2018-06-19 中国石油天然气股份有限公司 一种页岩含油量的测量方法
CN107917873B (zh) * 2017-12-05 2020-05-19 南京林业大学 一种沥青混合料抗油蚀性能的测试方法
DE102018213210A1 (de) 2018-08-07 2020-02-13 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren zur Reinigung mineralischer Feststoffe und Holzmaterialien, Vorrichtung für dieses Verfahren und deren Verwendung
CN111257159A (zh) * 2020-02-24 2020-06-09 成都理工大学 一种碳酸盐岩储层碳质沥青分散及去除效果的评价方法

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Publication number Priority date Publication date Assignee Title
US10640712B2 (en) 2016-11-18 2020-05-05 Stojan Kotefski Methods for retrieving, reclaiming, or recycling petroleum-based products and byproducts
US11549016B2 (en) 2016-11-18 2023-01-10 Stojan Kotefski Hybrid crude oil and methods of making the same using petroleum-based waste stream products
WO2018125952A1 (en) * 2016-12-30 2018-07-05 Stojan Kotefski Methods for reclaiming or recycling asphalt and asphalt and asphalt components produced thereby
CN112057884A (zh) * 2020-07-22 2020-12-11 江苏高速公路工程养护技术有限公司 一种沥青分子测试用流动液循环使用处理方法及系统
CN112057884B (zh) * 2020-07-22 2022-04-29 江苏高速公路工程养护技术有限公司 一种沥青分子测试用流动液循环使用处理方法及系统
WO2024084358A1 (en) * 2022-10-19 2024-04-25 Russell Atlas James System, method, and apparatus for recycling asphalt shingles

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DE112011102547A5 (de) 2013-05-02
EP2412783A1 (de) 2012-02-01
CA2806748A1 (en) 2012-02-02
WO2012013363A1 (de) 2012-02-02
CN103314077A (zh) 2013-09-18

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