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WO2011144322A2 - Procédé et installation de dépolymérisation de matières contenant des hydrocarbures - Google Patents

Procédé et installation de dépolymérisation de matières contenant des hydrocarbures Download PDF

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Publication number
WO2011144322A2
WO2011144322A2 PCT/EP2011/002445 EP2011002445W WO2011144322A2 WO 2011144322 A2 WO2011144322 A2 WO 2011144322A2 EP 2011002445 W EP2011002445 W EP 2011002445W WO 2011144322 A2 WO2011144322 A2 WO 2011144322A2
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WO
WIPO (PCT)
Prior art keywords
fraction
solid
reactor
liquid fraction
liquid
Prior art date
Application number
PCT/EP2011/002445
Other languages
German (de)
English (en)
Other versions
WO2011144322A3 (fr
Inventor
Dieter Wagels
Manfred Sappok
Original Assignee
Dieter Wagels
Manfred Sappok
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 Dieter Wagels, Manfred Sappok filed Critical Dieter Wagels
Priority to EP11741090A priority Critical patent/EP2572351A2/fr
Publication of WO2011144322A2 publication Critical patent/WO2011144322A2/fr
Publication of WO2011144322A3 publication Critical patent/WO2011144322A3/fr

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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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • 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
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/02—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in retorts
    • 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
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials

Definitions

  • the invention relates to a process and a plant for the depolymerization of materials containing hydrocarbons, such as residues, synthetic hydrocarbon-containing polymers or waste oil, in which the material is reacted in a cleavage reactor in a gaseous fraction and a bottom fraction.
  • materials containing hydrocarbons such as residues, synthetic hydrocarbon-containing polymers or waste oil
  • TECHNOLOGICAL BACKGROUND The depolymerization of materials containing hydrocarbons, particularly for the production of diesel oil, involves plastics, oils, fats, dried garbage, electric cables, wood, paper, digested sludge, agricultural debris, natural fibers, and many other waste or waste materials catalytically depolymerizes the target to obtain as few solid and gaseous conversion products. Catalysed depolymerization processes are common, as described, for example, in DE 103 16 969 A1 and DE 100 49 377 A1. For production reasons, a mixture of bitumen and oil is produced during depolymerization in the reactor. The bitumen must be continuous or discontinuous
  • CONFIRMATION COPY be removed from the process. This is usually done via a sump drain.
  • a disadvantage of the known method is that usually the right mixture of bitumen and oil can not be discharged. On the one hand, if too much bitumen-oil mixture is discharged as bottom product, the yield of produced oil decreases. On the other hand, if too little of the bottom product of a mixture of bitumen and oil is discharged, there is a risk that the bottom outlet will become clogged and coked.
  • the object of the present invention was to overcome this disadvantage and to develop an economical process and a plant to be operated economically, which does not have the aforementioned disadvantages.
  • the invention therefore provides a method having the features according to claim 1 and a system having the features according to claim 12 and the use of a device for separating solid and liquid fraction according to claim 21.
  • Advantageous embodiments are explained in detail in the subclaims and in the description ,
  • the invention thus relates to a process for the depolymerization of materials containing hydrocarbons, such as residues, plastics, synthetic hydrocarbon-containing polymers or waste oil, in which the material is heated to a temperature, and in liquid or pulpy consistency in one, heated to Spalttem- temperature Reactor, in particular a cleavage reactor, introduced, in particular injected under pressure, in particular continuously injected under pressure, and a gaseous fraction for further treatment is withdrawn from the reactor, and a bottom product is continuously or batchwise discharged from the reactor and the bottom product in a device is transferred to the separation of solid and liquid fraction and is separated in the apparatus for the separation of solid and liquid fraction into a liquid fraction and a solid-containing fraction.
  • hydrocarbons such as residues, plastics, synthetic hydrocarbon-containing polymers or waste oil
  • Suitable materials to be used in the process or in the plant according to the invention are, in particular, an oil, in particular used oil, fats, motor oils, dried waste, electric cables, wood, paper, digested sludge, agricultural residues, natural fibers and, in particular, generally all hydrocarbon-containing materials, as well as waste or waste materials which can be catalytically depolymerized with the aim of forming as few solid and gaseous conversion products.
  • the material contains at least one hydrocarbon or synthetic hydrocarbons containing polymer.
  • the method according to the invention it is possible to discharge the bottom product as a strong oily mixture for the separation of the bitumen from the reactor, and to separate this with discharged oil in the apparatus for separating solid and liquid fraction as a liquid fraction.
  • the bottom product consists in particular of a mixture of liquid and solid compounds and is free of steam or process gases.
  • the thus separated oil can be recycled as a liquid fraction according to the invention in the reactor.
  • the device for separating solid and liquid fraction is designed as a decanter, separator or centrifuge and the bottom product is transferred as centrifuged into the centrifuge and there in a liquid fraction, in particular waste oil fraction, and solid fraction contained separated.
  • the product to be centrifuged, as well as the liquid and solid fraction contain no gaseous or vaporous compounds under the conditions of separation in the apparatus for separating solid and liquid fractions.
  • the fraction containing solids is very bitumen-containing.
  • the centrifuged material can be fed continuously or discontinuously to the apparatus for separating solid and liquid fractions.
  • the resulting liquid fraction in turn, can be returned to the reactor continuously or discontinuously.
  • the return of the liquid fraction into the reactor can be carried out directly or indirectly.
  • the liquid fraction, in particular the waste oil-containing fraction recycled directly into the reactor and can be further cracked and purified by distillation. Indirect recycling of the liquid fraction into the reactor may suitably occur together with the preheated hydrocarbon containing material.
  • the liquid fraction fed to the reactor is further depolymerized in the reactor and treated by distillation together with the heating or diesel oil present in the reactor.
  • the separated, returned to the reactor oil thus increases the yield of heating or diesel oil.
  • the fraction containing solids separated via the apparatus for separating solid and liquid fractions comprises bitumen and can be adjusted to a consistency suitable for road construction, depending on the later intended use of the bitumen.
  • the consistency of the solids-containing fraction can be adjusted by varying the process parameters, such as the number of revolutions / minute of the centrifuge or the choice of process time, the parameters depending on the materials used, containing hydrocarbons, and their preparation. The person skilled in the art knows how to choose these parameters in individual cases.
  • a double flap system for discharging the bottom product into the apparatus for separating solid and liquid fraction is arranged between the reactor and the apparatus for separating solid and liquid fraction.
  • the double flap system is arranged in the region of the bottom of the reactor and allows the discharge of the bottom product in defined discontinuous or continuous amounts.
  • the apparatus for separating solid and liquid fractions can regularly be filled batchwise, depending on the spin time of the individual separation processes, repeatedly with centrifuged material.
  • the bottom product is more preferably transferred as a centrifuged product into the centrifuge with drive.
  • the device for separating solid and liquid fractions has the following components: a Centrifugal drum with drum shell and a screw with a screw body with a, a plurality of screw flights having screw blade, between the screw threads is formed a conveyor track for transporting the material to be processed centrifuged.
  • a drum space is provided with a cylindrical portion and is axially closed by a drum cover, in particular, the drum lid is conical.
  • the apparatus for separating solid and liquid fraction has an inlet for transferring the centrifuged material into the centrifugal drum and has at least one discharge for the solids-containing fraction and at least one discharge for the liquid fraction.
  • the drive can be used to adjust the centrifugal force for separation into the solids-containing fraction and the liquid fraction.
  • the device for the separation of solid and liquid fraction can be operated with different drives, which depend on the requirements of the centrifuged material and the fractions to be separated.
  • the simplest drive is a so-called O-drive in which a drum and differential speed control is not possible.
  • Another drive is a so-called interchangeable plate drive, in this drive, a second belt drive for driving the input shaft of the transmission is used via the main motor.
  • the differential speed is set depending on the drum speed and gear ratio.
  • a so-called 2-motor drive allows control of the differential speed over a large control range.
  • the second motor is connected to the input shaft of the transmission and sets this in rotation and thus generates depending on the drum speed and the gear ratio, the differential speed.
  • Other drives are the 2-gear drives, differential gear drives or the so-called hydro-drives.
  • the process of depolymerization, the reactor, the process parameters and the starting materials are described in WO 2006/092306 A1, the disclosure of which fully to the subject of the present invention is done. According to the method disclosed therein, the injection takes place at the beginning of the process, in particular under pressure, by means of an injection pump or an extruder screw, being used as an extruder screw, in particular one known from the plastic injection foundry.
  • the material is exposed to a pressure of between 100 and 1 bar, preferably between 100 and 2 bar, in this injection pump or extruder screw. Further, the material is preheated to a temperature above about 100 ° C, preferably to a temperature above about 250 ° C.
  • the preheating is preferably carried out in two stages, wherein in a first stage the material is heated to a temperature of about 100 ° C to 150 ° C by kneading and compressing to remove gases and interstitial volumes and in a second stage with simultaneous pressure build-up Preheating to about 200 ° C to 300 ° C takes place.
  • the first preheating stage is preferably followed first by a pressure relief stage for the separation of vapors, such as water vapor.
  • the reactor temperature on the inner wall of the reactor during the depolymerization is preferably 300 ° C. to 460 ° C., preferably between 340 ° C. and 440 ° C., and very particularly preferably between 390 ° C. and 420 ° C. It is further preferred that the material is supplied to the depolymerization at a distance from the reactor inner wall, in particular in a central region of the reactor. Preferably, the material is introduced directly into the liquid.
  • the reactor or cleavage reactor preferably has a scraping device for cyclically cleaning at least the liquid-covered reactor inner walls during the depolymerization process, in particular as described in WO 2006/092306.
  • the reactor preferably has a multi-leaf rotating or rotatable mixer or stirrer with arms and wings.
  • the wings are at least partially made of temperature-resistant ceramic or graphite material.
  • the wings of the inner wall contour of the cleavage reactor are substantially simulated.
  • a cleavage reactor is used in the process and in the plant which corresponds to that in WO 2006/092306. According to the invention, the process is carried out so that the bottom product is transferred into the apparatus for the separation of solid and liquid fraction.
  • the centrifuged material is transferred to the centrifugal drum, which via a drive to more than 1,000 revolutions / min. is set.
  • the device for the separation of solid and liquid fraction with more than 1,000 revolutions / min. operated, preferably with over 2000 to 10,000 revolutions, more preferably with 2,500 to 7,000 revolutions / minutes, preferred alternative speed ranges are between 2500 to 3000 revolutions / minute or 5000 to 7000 revolutions / minute.
  • the apparatus for separating solid and liquid fraction with about 2500 to 3000 revolutions / min. +/- 500 revolutions / min. operated.
  • the apparatus for separating solid and liquid fraction with 5500 to 6500 in particular operated at 6000 revolutions / minute.
  • the person skilled in the art knows how to adjust the correct setting per minute as a function of the material introduced and the withdrawn bottom product and the other process parameters in order to obtain an optimum separation of the fraction containing solids and the liquid fraction.
  • the mixture of the bottom product always depends on the process control and the material used in each case.
  • the aim is always to recover as much oil in this process step from the bottom product, which can be recycled to the reactor in order to obtain a particularly good yield in the overall process.
  • the viscosity of the solids-containing fraction can be adjusted over the residence time and the revolutions / minute of the centrifuge, otherwise depending on the registered bottom product.
  • the process temperature at which the device is operated for the separation of solid and liquid fraction is between 150 to 450 ° C, according to the invention between 180 to 220 ° C, in particular by 200 ° C. In individual cases, a temperature range of 350 to 450 ° C can be set.
  • the residence time in the apparatus for separating solid and liquid fraction may be between 10 seconds to 2 hours, in particular between 1 minute to 1 hour, preferably between 2 minutes and 30 minutes, especially between about 5 to 10 minutes.
  • the viscosity of the bitumen obtained according to these process conditions is suitable for road construction.
  • the bitumen obtained as a fraction containing solid material complies with the standards DIN EN 12591 and TL bitumen STB07, in particular the penetration test.
  • the product to be centrifuged is preferably in the apparatus for separating solid and liquid fraction, which is designed as a decanter, centrifuge or separator, at about 1000 to 10,000 revolutions / minute at 150 to 400 ° C over a residence time of 10 seconds to 1 hour.
  • a residence time of 5 to 10 minutes at 2500 to 3000 revolutions / minute at about 200 ° C (plus / minus 20 ° C) can be obtained according to the invention as a solid fraction containing a, suitable for road construction, bitumen.
  • the discharge of the bottom product from the reactor can be carried out continuously or batchwise.
  • the bottom product is discharged from the reactor batchwise in accordance with the residence times of the bottom product as a centrifuged product in the apparatus for separating solid and liquid fractions.
  • the bottoms product can also be continuously discharged.
  • different types of apparatus for separating solid and liquid fractions such as separators, centrifuges or decanters, can be used in parallel.
  • the apparatus for separating solid and liquid fractions is designed as a centrifuge, which is selected from a group consisting of three-column centrifuges, Einpufferzentrifugen, Gleitschwingzentrifugen, rocking centrifuges (tumbling centrifuges), Vollmantel-peeling centrifuges, solid bowl centrifuges, tube centrifuges, Siebtrommel Centrifugal centrifuges, pusher centrifuges, screw centrifuges, chip centrifuges, inverting filter centrifuges, disc centrifuges or universal centrifuges.
  • a centrifuge which is selected from a group consisting of three-column centrifuges, Einpufferzentrifugen, Gleitschwingzentrifugen, rocking centrifuges (tumbling centrifuges), Vollmantel-peeling centrifuges, solid bowl centrifuges, tube centrifuges, Siebtrommel Centrifugal centrifuges, pusher centrifuges
  • a separator for separating the solid and liquid fractions is used. Separators work on the principle of centrifuges. Centrifugal forces in a rotating drum separate solids or higher density liquids from lower density liquids. Separators differ from centrifuges in that semi (semi-) or fully continuous operation is possible. As a result, high separation efficiencies based on the volume flow are achieved with small dimensions.
  • the heavy residues (solid particles) accumulate inside the drum at the largest diameter. If an automatic emptying system is present in the machine, the separated solids are released from the drum body by axial lowering of a component in the drum after a corresponding time (depending on solids volume fraction in the inlet, sludge volume capacity of the drum and inflow quantity) Slide) and associated release of the opening slots of the drum body from the separator with the help of the existing kinetic energy ejected / shot out.
  • the liquid phases are removed from the machine via a scraper system (gripper).
  • the separator is selected from a group consisting of nozzle separators, press screw separators, chamber separators, disk separators or Vollmanteltellerseparatoren.
  • the selection of the device to be used for the separation of the solid and liquid fraction is effected in this case in particular with regard to the particle size of the solids to be separated.
  • disk centrifuges are used at particle sizes of 0.5 to 500 pm.
  • separation capacity is 5000 to 13000 g possible.
  • decanters are used at particle sizes of 15 ⁇ to 20 mm.
  • the separation efficiency is in the range of 1500 to 4000 g.
  • the type of centrifuge to be used for separation can also be selected.
  • a centrifuge with self-cleaning drum can be used.
  • a centrifuge with nozzle drum can be used.
  • first a separation of the solid and liquid fraction by a separator wherein the solid fraction is discharged.
  • the solid fraction is then transferred to a decanter where further separation of the liquid fraction occurs.
  • the liquid fraction obtained from the separator and decanter is then again subjected to centrifugation, for example with a disk centrifuge, to increase the yield, a separation capacity of between 5000 and 13000 g being achieved.
  • the solids content obtained in the disc centrifuge can in turn be fed to the decanter. This creates a redundant system that allows continuous separation of solid and liquid fractions while ensuring increased yield of the depolymerization process.
  • a sieve such as a curved sieve or an arrangement of several sieves with descending mesh spacing.
  • the thereby separated liquid fraction is then fed to a further separation by means of a separator or a centrifuge. It is also conceivable to supply the liquid fraction to the decanter.
  • the solid fraction separated off via the sieve can subsequently be fed to a separation via a separator, centrifuge or decanter, depending on the solids content.
  • the invention also provides a system for the depolymerization of materials containing hydrocarbons, in particular for carrying out the method according to any one of claims 1 to 11, wherein as materials in particular residues, plastics or used oils are used.
  • the plant for the depolymerization of materials containing hydrocarbons comprises a device for preheating liquid, paste-like and / or solid materials containing hydrocarbons, a heated cleavage reactor with associated distillation column.
  • the distillation column is preferably assigned directly to the cleavage reactor, for example, it is placed on top of the cleavage reactor.
  • the cleavage reactor has at least one feed for feeding the preheated, liquid or pasty material into the cleavage reactor and a bottom outlet for discharging sump products.
  • the sump outlet is further associated with a device for separating a solid and a liquid fraction, which has at least one discharge for the solids-containing fraction and at least one discharge for the liquid fraction. It is particularly preferred if the device for separating a solid and a liquid fraction via the discharge for the liquid fraction is directly or indirectly connected to the reactor to allow a return of the separated liquid fraction in the reactor.
  • the device for separating a solid and a liquid fraction may be embodied according to the invention as a separator, centrifuge or decanter.
  • the discharge of the apparatus for separating a solid and a liquid fraction is connected to the reactor for recycling the separated liquid fraction to the reactor.
  • the discharge may also be connected to the device for preheating in order, via the device, to return the liquid fraction, in particular the waste oil fraction, indirectly to the reactor.
  • the device for separating a solid and a liquid fraction may be designed so that a separation by sedimentation and sedimentation alone is allowed in a waste oil and in a bitumen-containing fraction.
  • Such a configured device for separating a solid and a liquid fraction may be a conventional container with a feed and a drain, in which the drained bottoms fraction can be transferred and there is a solid / liquid separation over time by the density differences. The heavier can then be discharged in the usual way down the bottom of the container, while the lighter, in particular waste oil-containing phase can be recycled directly or indirectly into the reactor.
  • Such a container may also be a container with at least one internal separating step, which is at least one wall disposed in the container, which is connected to the inner sides of the container and at the bottom tightly connected to the container and on the upper edge of the bottom product can flow slowly ,
  • the two chambers formed by this measure can be used as separation stages.
  • a decanter which is designed as a two- or three-phase decanter.
  • a decanter In a decanter (decanter centrifuge), the solid components of the substances to be separated with a slower or faster-running auger steadily removed from the centrifuge drum.
  • the decanter (decanter centrifuge) is usually used at higher solids content (from about 3% in the inlet).
  • a solid / liquid separation takes place. Solids and liquid are discharged continuously.
  • An advanced design is the 3-phase decanter. Here, solids and two different non-dissolvable liquids are separated.
  • the plant according to the invention comprises for the depolymerization of materials containing hydrocarbons, a device for preheating liquid, pasty and / or solid materials containing hydrocarbons, a heated cleavage reactor with associated distillation column.
  • the cleavage reactor has at least one feed for feeding the preheated, liquid or pulpy material into the cleavage reactor and a bottom outlet for discharging bottom product.
  • the bottom outlet is assigned to the centrifuge, which has at least one discharge for the solids-containing fraction and at least one discharge for the liquid fraction.
  • the centrifuge is associated with a drive and a centrifugal drum.
  • the sump product is transferred as a centrifugal product into the centrifuge via an inlet into the centrifugal drum.
  • the centrifugal drum on a drum shell and a screw with a screw body which is provided with a, a plurality of screw flights having screw blade. Between the flights a conveyor track for transporting the material to be processed is formed.
  • the centrifuge has a drum space with a cylindrical portion.
  • the drum space is axially closed by a drum cover, in particular the drum lid is conical.
  • the centrifuge has at least one discharge for the solids-containing fraction and at least one discharge for the liquid fraction. More preferably, the liquid fraction fraction of the centrifuge is connected to the reactor to recycle the separated liquid fraction into the reactor.
  • the device for separating solid and liquid fractions is designed and suitable for treating the material to be centrifuged preferably at about 1000 to 10,000 revolutions / minute at 150 to 450 ° C. for a residence time of 10 seconds to 1 hour.
  • the centrifuged material is treated for a residence time of 5 to 10 minutes at 2500 to 3000 revolutions / minute at about 200 ° C (plus / minus 20 ° C).
  • a solid-containing fraction can then be obtained, suitable for road construction, bitumen.
  • the centrifuges are selected from a group consisting of three-column centrifuges, single-buffer centrifuges, floating oscillators. Centrifuges, vibrating centrifuges (tumbling centrifuges), solid bowl peeler centrifuges, solid bowl centrifuges, tube centrifuges, sieve drum centrifuges
  • Centrifugal centrifuges pusher centrifuges, screw centrifuges, chip centrifuges, inverting filter centrifuges, disc centrifuges or universal centrifuges.
  • the bottom outlet of the reactor is assigned a double-chamber system via which the bottom product can be discharged, wherein the discharged bottom product can be supplied by means of a feed line to the apparatus for separating solid and liquid fractions.
  • the double flap system particularly preferably comprises the bottom outlet of the reactor and a downstream container, the container having a first outlet for transferring at least a portion of the discharged bottom product into the apparatus for separating solid and liquid fraction and optionally a second outlet.
  • the second drain can be used in particular to discharge high-pasty sump products from the container.
  • the reactor in the area of the sump outlet is concave, conical or concave to conical shaped to discharge the sump products and / or the container is bottom-shaped concave, conical or concave to conical shaped to the second drain.
  • the reactor is preferably a cleavage reactor with an attached distillation column, the reactor preferably being equipped with a scraping device and / or mixer or stirrer.
  • a cleavage reactor is used in the process and in the plant which corresponds to that in WO 2006/092306.
  • the reactor is preferably not a turbine or extruder screw or a reactive distillation column.
  • At least one screen such as a curved screen, is initially provided for a coarse separation of the solid and liquid fractions.
  • a coarse separation is already possible in the first step.
  • an arrangement of a plurality of sieves with descending mesh spacing is provided, wherein the liquid fraction is subjected to a continuous coarse separation prior to transfer to separator, centrifuge or extractor. The liquid fraction thus obtained can then be subjected to a fine separation by means of centrifugation.
  • a separator or a centrifuge is provided. It is also conceivable to supply the liquid fraction to a decanter.
  • the cleavage reactor is associated with a double flap system, via which the bottom product can be discharged, and the drained bottoms product can be supplied by means of a feed line of the device for separating a solid and a liquid fraction.
  • the invention also provides the use of a device for the separation of solid and liquid phase, this device is designed as a decanter, centrifuge or separator, downstream of the cleavage reactor for separating a liquid fraction, in particular an oil-containing fraction, and a solid-containing fraction, especially bitumen-containing fraction, in a polymerization process.
  • Fig. 1 is an overview of the practical structure of a depolymerization risationsstrom
  • Fig. 2 is a schematic representation of the centrifuge 1 b.
  • FIG. 1 shows a schematic representation of a possible structure of a depolymerization plant.
  • the preheating of the raw material takes place in a conveyor and compressor screw 14 by external heating and / or friction.
  • various raw materials are supplied at different points, such as plastics, oils, in particular Al flushing oils, and optionally additives.
  • After at least partial preheating is a pressure release.
  • water vapor and other gases can be removed via an exhaust duct, e.g. a filter, fed or discharged.
  • the liquid or slurry raw material is conveyed further by means of a screw conveyor with optionally further heating and generation of internal pressure and fed into the interior of a pot-shaped, externally heated depolymerization or cleavage reactor 12 via a feed 15.
  • a distillation column 16 is mounted, which is a head capacitor and a product tank, for example, for heating oil / diesel, downstream.
  • a spent oil and bitumen-containing bottoms product can be discharged at a sump outlet 13 from the reactor.
  • the discharge of the The double flap system comprises the bottom outlet 13 of the reactor 12 and a downstream container 17, wherein the container 17, a first outlet 17a for transferring at least a portion of the discharged bottom product in a device for separating a solid and a liquid fraction 1 or a centrifuge 1a is assigned.
  • the container 17 additionally has a second outlet 17b in order to be able to remove mixtures of bitumen-containing mixtures which have optionally been deposited therefrom directly from the container.
  • FIG. 2 schematically shows the centrifuge 1a in axial section, namely a screw centrifuge for separating the bottom product, which is discharged at the bottom outlet, in particular via the double flap system 18, and via the outlet / supply line 17a, 19 (FIG. 1) as a centrifuged product into a centrifugal drum 6 is registered.
  • the centrifuge 1a is driven by a drive 2 about its longitudinal axis A.
  • the bottom product is introduced as a centrifugal product via an inlet 9.
  • the centrifugal drum has a drum shell 1 and a screw 3.
  • the screw 3 is provided with a screw body 4 and a screw blade 5 having a plurality of screw flights.
  • a conveyor track is formed between the flights, which is designed for transporting the sling to be processed.
  • the centrifuge 1a has a drum space 7 with a cylindrical section closed axially by a drum cover 8. Via at least one discharge 10 of the centrifuge 1a, a fraction containing solids can be removed at the drive end of the drum.
  • the centrifuge has at least one discharge 11 at the opposite (entry-side) end of the drum.
  • the centrifuged material can be fed continuously or discontinuously via the inlet 9 of the rotating at high speed drum. Due to the centrifugal force, the solids-containing fraction, especially the bitumen containing fraction, down on the drum inner wall.
  • the solids-containing fraction is scraped off by the screw blade 5 of the screw body 4 and conveyed by it to the discharge 10 (solids discharge).
  • the screw body with screw blade is preferably designed as a hard metal-armored screw conveyor 4, 5.
  • the separated liquid fraction is conveyed to the discharge 11 (liquid discharge). There, the liquid fraction can emerge free-flowing or under pressure by using a corresponding paring disc.
  • the drive 2 can have a motor.
  • the engine has a power of 10 kw to 250 kW. Typical power ranges are between 10 kW to 15 kw, between 22 to 35 kw or between 1 10 kw to 250 kw.
  • the device for separating a solid and a liquid fraction 1 is designed as a separator.
  • the device for separating a solid and a liquid fraction 1 is designed as a decanter, wherein a separation of the solid fraction of the liquid fraction takes place at particle sizes of 15 pm to 20 mm.
  • the separation efficiency is in the range of 1500 to 4000 g.
  • the sump material can be centrifuged. Probably due to different particle sizes, some of the substances sediment as a soft cake. In these soft cake is probably a larger amount of oil remain bound in the solid.

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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)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé et une installation de dépolymérisation de matières contenant des hydrocarbures, telles que des matières résiduelles, des polymères synthétiques contenant des hydrocarbures ou des huiles usagées. Selon l'invention, la matière est transformée en une fraction gazeuse et une fraction de fond dans un réacteur de fission, puis la fraction de fond est séparée en une fraction liquide et une fraction contenant des matières solides dans un dispositif pour séparer une fraction solide et une fraction liquide.
PCT/EP2011/002445 2010-05-17 2011-05-17 Procédé et installation de dépolymérisation de matières contenant des hydrocarbures WO2011144322A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP11741090A EP2572351A2 (fr) 2010-05-17 2011-05-17 Procédé et installation de dépolymérisation de matières contenant des hydrocarbures

Applications Claiming Priority (2)

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DE102010020707.1 2010-05-17
DE102010020707 2010-05-17

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WO2011144322A2 true WO2011144322A2 (fr) 2011-11-24
WO2011144322A3 WO2011144322A3 (fr) 2012-01-12

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EP (1) EP2572351A2 (fr)
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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19629714C1 (de) 1996-07-25 1998-01-22 Heraeus Noblelight Gmbh Verfahren zur Herstellung von Anschlußkontakten für Strahler mit Quarzglas-Kolben

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1991010619A1 (fr) * 1990-01-11 1991-07-25 Koa Oil Company, Limited Production d'articles moules en graphite elastiques
DE4428355A1 (de) * 1994-05-20 1996-02-15 Veba Oel Ag Vorrichtung zur Depolymerisation von Alt- und Abfallkunststoffen
CN1159821A (zh) * 1994-10-04 1997-09-17 维巴石油有限公司 从废旧塑料中获得化学原料和燃料组分的方法
US8518243B2 (en) * 2004-10-01 2013-08-27 Saudi Arabian Oil Company Method for utilizing hydrocarbon waste materials as fuel and feedstock
WO2006117006A1 (fr) * 2005-05-03 2006-11-09 Danmarks Tekniske Universitet Procede et unite mobile de ramassage et pyrolyse de biomasse
ITBO20070104A1 (it) * 2007-02-21 2008-08-22 Kdvsistemi Brevetti S R L Apparato per la produzione di combustibile sintetico

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19629714C1 (de) 1996-07-25 1998-01-22 Heraeus Noblelight Gmbh Verfahren zur Herstellung von Anschlußkontakten für Strahler mit Quarzglas-Kolben

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EP2572351A2 (fr) 2013-03-27
WO2011144322A3 (fr) 2012-01-12

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