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
  • C10G1/02—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
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
  • C10B47/28—Other processes
  • C10B47/32—Other processes in ovens with mechanical conveying means
  • C10B47/34—Other processes in ovens with mechanical conveying means with rotary scraping devices
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
  • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
• • 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
  • 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
  • C10G9/005—Coking (in order to produce liquid products mainly)
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/04—Diesel oil
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/141—Feedstock
  • Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics

Definitions

• the invention relates to hydrocarbon extraction from mineral oil and carbon based raw materials and residues in a continuous fashion.
• the invention relates to a method for the depolymerisation of hydrocarbon- containing residues or material, especially for the production of diesel oil and/or heating oil.
• the depolymerisation process i.e., the molecule-shortening of the long-chained hydrocarbon compounds
• the hydrocarbon molecules settle on the catalysts until they have reached the reaction temperature-dependent on the type of residue-and the degradation products vaporize.
• a fluid/catalyst mixture is conducted in a cycle between the evaporation temperature and the raw-material feed-in temperature. By feeding in raw material, the mixture temperature is lowered. The evaporation temperature of the desired and lower boiling fractions are reached again in a heater, such as a tubular heat exchanger, following in the cycle.
• the components remaining as a liquid are fed back to the raw-material feed-in.
• the agglomerations forming from catalyst material and higher boiling components of the raw material in this cycle process are transferred outward for further processing.
• the vapour fraction leaving the cycle is fractionated in a distillation system, producing, e.g., diesel oil or heating oil. Gaseous components are combusted under the production of hot combustion gases, which provide the quantity of heat necessary for evaporation, and the process temperature (cracking temperature) in the liquid cycle. If the raw material contains chlorine, sulphur, phosphorus, and/or other components that are not desired in the product (diesel oil or heating oil), these are removed in the cycle process.
• the present invention aims to provide a simple system and method to overcome the above mentioned problems.
• a system for the depolymerisation of hydro-carbon containing material for producing diesel oil and/or heating oil comprising:
• the desired temperature range operates in the range of 390 to 420 degrees C.
• means for removing heated raw material after vapour extraction from said reactor at intervals to a holding and cooling storage vessel are provided.
• the reactor comprises a heating jacket provided substantially around the reactor to define a heating space between the outer surface of the reactor and the inner surface of jacket.
• said means for heating comprises means for hot gas to be supplied from a burner and blower system through an inlet to the heating space.
• the reactor is substantially cylindrical in shape and the means for evenly distributing the material comprises a rotor blade rotating about an axis of said reactor.
• said blade is dimensioned to provide a gap between the inner surface of the reactor and the end of the blade to define the thickness of the film of heated raw material.
• the gap is selected to generate a highly turbulent zone to provide for high the transfer values to allow vapour to be extracted to the evaporator area.
• the reactor is conical shaped such that the heated raw material being processed is continuously fed into the largest diameter of the reactor and spread towards the shortest diameter end of the reactor.
• the reactor comprises a short path distillation column.
• a process for the depolymerisation of hydro-carbon containing material for producing diesel oil and/or heating oil comprising the steps of: pre-heating raw hydro-carbon containing material to a fluidic or viscous state and introducing said pre-heated material under pressure into a reactor; further heating of the raw material under vacuum in said reactor such that that the raw material under vacuum is heated to a desired temperature range;
• a system for the depolymerisation of hydrocarbon-containing material for producing diesel oil and/or heating oil comprising a reactor or short path distillation column adapted to exceed temperature operation of 390 degrees Celsius and provided with a plant specific exothermal heat source.
• raw materials enter the column in a liquid or viscous state by pre-heating and introducing it under pressure to a specially adapted device where further heating of the raw material takes place under vacuum.
• vapour fraction is continually drawn off and means for releasing solid residues at intervals to a holding and cooling storage vessel.
• the short path distillation column can be adapted to accommodate the heating mode and to accept the increase temperature in a heating jacket provided around the short path distillation column.
• the short path distillation column provides for hot gas to be supplied from a purpose built burner and blower system.
• the short path distillation column is provided with means for the removal of residue from the interior walls of the column, thus enabling a constant and stable heating of the raw material and a high conversion rate.
• the short path distillation column is provided with means for removal of residue or solid fraction periodically through an isolating valve system and means for transporting away from the reactor via an extrusion screw to a cooling storage vessel.
• the short path distillation column is provided with means to control the mass balance at the vapour stage.
• Figure 1 is a block diagram circuit of a system for the depolymerisation of hydrocarbon-containing material for producing diesel oil and/or heating oil;
• Figure 2 is a 3D perspective view of a system for the depolymerisation of hydrocarbon-containing material for producing diesel oil and/or heating oil, according to a preferred embodiment of the invention ;
• FIG. 3 illustrates a reactor according to the invention
• Figure 4 illustrates a second reactor according to another aspect of the invention
• Figure 5 illustrates a third reactor according to a further aspect of the invention
• Figure 6 illustrates a cut through view of the reactor of Figures 3 to 5
• Figure 7 illustrates a second cut through view of the reactor of Figures 3 to 5;
• Figure 8 illustrates a fourth reactor according to another aspect of the invention
• Figure 9 is a 3D perspective view of a system for the depolymerisation of hydrocarbon-containing for producing diesel oil and/or heating oil, according to another embodiment of the invention.
• Figure 1 is a block diagram circuit of a system for the depolymerisation of hydrocarbon-containing material for producing diesel oil and/or heating oil.
• Figure 1 shows that raw material 1 composed of plastics and waste oil is heated in a preheating stage 2 to 250[deg.] C. and then fed to a device for pressure injection, such as a pressure and feed pump (injection 3) known for the injection moulding of plastic.
• This pump permits the direct injection of the raw material into a reactor 4, whose liquid contents are kept by a heater 5 (with, e.g., oil or gas and an exhaust-gas temperature of approximately 800[deg.] C.) at a temperature between approximately 300[deg.] C. and 460[deg.] C, preferably between 340[deg.] C. and 440[deg.] C, and its waste heat is recovered partially in the preheating stage 2, e.g., a recuperative heater.
• a heater 5 with, e.g., oil or gas and an exhaust-gas
• the reactor 4 can be built in various ways and sizes. Similarly, there are no narrow restrictions for the heater 5.
• FIG. 2 is a 3D perspective view of a system for the depolymerisation of hydrocarbon-containing for producing diesel oil and/or heating oil, according to a preferred embodiment of the invention, indicated generally by the reference numeral 10.
• a reactor 1 1 is provided where raw hydro-carbon containing material is pre-heated to a fluidic or viscous state and introduced under pressure into the reactor 1 1 .
• Means 12 for further heating of the raw material under vacuum in said distillation column is provided using a burner, such that that the raw material under vacuum is heated to a desired temperature range to a temperature of between 390 and 420 degrees C. Vapour from said heated raw material is channelled to an evaporator or condenser area 13. The vapour is condensed and channelled off to a holding area 14, thus producing said diesel oil or heating oil.
• FIG. 3 An important aspect of the invention is shown in Figures 3 that illustrates a more detailed view of the reactor, indicated generally by the reference numeral 30 which has been adapted to exceed normal temperature operation and comprises a plant specific exothermal heat source.
• Raw material in a viscous state is fed into the reactor through inlet 31 under pressure.
• the temperature is now raised to the operating range of 390 to 420 degrees C. It was surprisingly found that this is the optimum temperature to extract the vapours produced.
• This increase in temperature is achieved by using a specially designed burner and blower system by delivering hot gas fed in through a hot gas inlet 32, thus heating the process by hot exhaust gas (approx 800 degrees C).
• the excess heat produced is diverted out through an exhaust gas outlet 33 and used to pre-heat the raw material in the extrusion phase in a closed loop system arrangement.
• Condensing coolant can be introduced into the reactor though inlet 34 and outlet 35.
• the vapours or gaseous fractions are distilled at the relative fraction for fuel oil or diesel through outlet 36. During the vapour stage gases that do not convert to fuel oil or diesel are drawn off 37 and are used in fuelling the exothermal heat system, this gas fraction is approximately 3-5% of the raw material used.
• the system provides for hot gas to be supplied from the purpose built burner and blower system.
• the reactor 30 can be adapted to accommodate the heating mode and to accept the increase temperature in a heating jacket provided around the reactor.
• Figure 4 illustrates a vertical reactor indicated generally by the reference numeral 40, where the raw material product being processed is continuously fed in above a heating jacket and evenly distributed onto the heating surface by a distribution ring, as described below in detail with respect to Figures 6 and 7.
• the product is picked up by rotor blades and is immediately spread over the heating wall as a highly turbulent thin film.
• the volatile components evaporate quickly and flow in a counter current to the fluid upwards and pass the rotating separator. Entrained droplets or lather are here ejected and flow back into an evaporator area.
• the low boilers product gases freed from any liquid constituents
• Thin Film Evaporators can be used which work using the Parallel Flow Principle.
• FIG. 5 illustrates a vertical conical type reactor that can be used in the system and process of the present invention, indicated generally by the reference numeral 50.
• the reactor of the present invention is designed to incorporate removal of residue from the interior walls of the column, thus enabling a constant and stable heating of the raw material and a high conversion rate. This can be achieved by a raw material scraper 61 , as shown in Figure 6.
• the residue or solid fraction is removed periodically through an isolating valve system and is transported away from the reactor via an extrusion screw to a cooling storage vessel.
• Figure 7 illustrates a second cut through view of the reactor of Figures 3 to 5.
• the preheated fluidic type viscous material comes into touch with a rotor after entering the distillation column it is picked up by a distribution ring and evenly distributed onto to the circumference 71 . Then it is gathered by the first rotor blades 72 which are lying beneath and is distributed onto the heated wall as a thin film (preferably sized 0.5 - 3.5 mm) and can be rotated in a clockwise or counter clockwise direction.
• the fluid builds a bow wave in front of every rotor blade, as shown in Section II of Figure 7.
• This bow wave is picked up by the rotor blade and migrates in the gap 73 between rotor and wall into a highly turbulent zone where an intense heat and mass exchange is happening in a radial direction.
• the highly turbulent condition provides for high heat transfer values in viscous fluids. Even temperature sensitive products are protected from overheating through the intense product mix in the bow wave. This counteracts against a debris build up on the heating surface.
• the process consists of the following production phases:
• the process consists of the following production phases:
• Figure 8 illustrates a fourth reactor according to another aspect of the invention where the reactor is place horizontal to the ground in operation, indicated generally by the reference numeral 80.
• the product being processed is continuously being fed into the largest diameter of the evaporator, is being picked up by the rotor blades and immediately spread over the heating wall as a highly turbulent thin film.
• the centrifugal forces which impacts the surrounding fluid ring is split into a force component vertical to the heating wall and into one in the direction of the largest diameter.
• a fluid backlog in the direction of the product inlet tube is created.
• the higher pressure of the fluid at the feeding tube carries the circulating fluid ring towards the smaller diameter.
• Figure 9 illustrates is a 3D perspective view of a system for the depolymerisation of hydrocarbon-containing for producing diesel oil and/or heating oil indicated generally by the reference numeral 90 similar to Figure 1 and hereinbefore described, except the reactor is placed horizontal to the ground.
• the system can be controlled by a specially designed software programme enabling the system to run in continuous mode.
• the complete process is controlled by a specially designed software package.
• This package enables the operator to control the mass balance at the vapour stage and allows conversion in a continuous fashion.
• the embodiments in the invention described with reference to the drawings comprise a computer apparatus and/or processes performed in a computer apparatus to control the system and method of the present invention.
• the invention also extends to computer programs, particularly computer programs stored on or in a carrier adapted to bring the invention into practice.
• the program may be in the form of source code, object code, or a code intermediate source and object code, such as in partially compiled form or in any other form suitable for use in the implementation of the method according to the invention.
• the carrier may comprise a storage medium such as ROM, e.g. CD ROM, or magnetic recording medium, e.g. a floppy disk or hard disk.
• the carrier may be an electrical or optical signal which may be transmitted via an electrical or an optical cable or by radio or other means.

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• Chemical & Material Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Engineering & Computer Science (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Chemical & Material Sciences (AREA)
• Physics & Mathematics (AREA)
• Thermal Sciences (AREA)
• Materials Engineering (AREA)
• Life Sciences & Earth Sciences (AREA)
• Wood Science & Technology (AREA)
• Combustion & Propulsion (AREA)
• Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Extraction Or Liquid Replacement (AREA)

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• 2011
  • 2011-04-26 US US13/642,942 patent/US20130158309A1/en not_active Abandoned
  • 2011-04-26 BR BR112012027180A patent/BR112012027180A2/pt not_active IP Right Cessation
  • 2011-04-26 AU AU2011244247A patent/AU2011244247A1/en not_active Abandoned
  • 2011-04-26 IE IE20110203A patent/IES20110203A2/en not_active IP Right Cessation
  • 2011-04-26 EP EP11721447.8A patent/EP2585557A2/de not_active Withdrawn
  • 2011-04-26 WO PCT/EP2011/056577 patent/WO2011131793A2/en active Application Filing
  • 2011-04-26 CA CA2797282A patent/CA2797282A1/en not_active Abandoned

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