Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
  • B01D3/14—Fractional distillation or use of a fractionation or rectification column
  • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
  • B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D1/00—Evaporating
  • B01D1/0011—Heating features
  • B01D1/0041—Use of fluids
  • B01D1/0052—Use of a liquid transfer medium or intermediate fluid, e.g. bain-marie
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D1/00—Evaporating
  • B01D1/02—Evaporators with heating coils
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D1/00—Evaporating
  • B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D1/00—Evaporating
  • B01D1/30—Accessories for evaporators ; Constructional details thereof
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D1/00—Evaporating
  • B01D1/30—Accessories for evaporators ; Constructional details thereof
  • B01D1/305—Demister (vapour-liquid separation)
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
  • B01D3/06—Flash distillation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
  • B01D3/14—Fractional distillation or use of a fractionation or rectification column
  • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
  • B01D3/322—Reboiler specifications
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G7/00—Distillation of hydrocarbon oils
  • C10G7/006—Distillation of hydrocarbon oils of waste oils other than lubricating oils, e.g. PCB's containing 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
  • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
• • 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
  • C10G2300/1007—Used oils

Definitions

• Waste oil The invention relates to the processing of
• polluted waste oil liquid oil-containing residues such as waste oil, polluted diesel, heating oil or shipping oils, here collectively referred to as polluted waste oil, which as
• the waste oil can be cleaned by pure distillation without changing the molecular structures.
• the invention can also be used in a temperature range
• the invention relates to a method for cleaning contaminated waste oil, in the starting material up to
• the invention also relates to a device for cleaning contaminated waste oil with a main reactor and a rectification column connected to it.
• DE 198 20 635 A1 discloses a process for the treatment of waste oil, in which the waste oil is subjected to a rough cleaning and subsequent drying, then thermally cracked at 400 to 500 ° C. and the cracking product is subjected to a distillation. Alkaline compounds are added to the pre-cleaned waste oil to lower the chlorine content added.
• the starting material comes into contact with a hot gas via a heat exchanger.
• DE 10 2012 008 458 A1 discloses a reactor for gasifying starting material, which is filled with a filler and a metal, which can be brought into the liquid phase by external heating elements.
• the base material is introduced into the bottom of this liquid metal bath. It is intended to use solid starting material in granular form. This starting material will undergo depolymerization due to the temperature of the metal bath.
• the source material goes into the
• EP 0 592 057 B1 describes a process in which solid starting material is also subjected to pyrolysis in a metal bath.
• WO 2014/106650 A2 describes a process for the oiling of hydrocarbon-containing starting material, likewise in a metal bath.
• the invention has for its object to provide a method and apparatus for cleaning contaminated waste oil, which enables efficient work even in very small systems, so that a compact system configuration and thus in particular a mobile use by a
• Container construction is made possible.
• the invention also lies the task is based on the effort for maintenance
• Fuel is transformed.
• the process can use known processes from the crude oil industry with a depolymerization process designed according to the invention
• Plastics are usually made from petroleum and - to put it simply - their hydrocarbons are chained together (polymerization) in such a way that solid materials become from a formerly liquid substance. The depolymerization reverses this process. The chains are through
• oils medium length
• waxes somewhat longer chains, also liquid when heated
• gases very short chains
• the object of the invention is achieved in that the waste oil is used as the starting material and an evaporation by at least indirect contacting of the starting material with a molten bath, the
• the used oil is distilled in the process.
• the special energy input system in the main reactor ensures that the waste oil is heated very quickly and in a controllable manner.
• flash evaporation is carried out in that the starting material is fed directly to the weld pool. This flash evaporation takes place within a few milliseconds. Flash evaporation or flash pyrolysis separates contaminants and uniquely efficiently transfers the oil fraction into the gas phase.
• Another embodiment of the method according to the invention provides for the starting material to be fed indirectly to the molten bath by passing it through the molten bath without a direct connection and via a heat-conducting connection.
• Waste This can be used for bitumen production in road construction or as a substitute fuel. There is no further waste.
• the object according to the invention is achieved in that the main reactor is designed as a molten bath evaporator, in that a reactor space with a
• Heating device is provided and an inlet in the reactor is arranged for the waste oil.
• a direct heat-conducting connection between the waste oil and the molten bath can be realized in the reactor space by directly entering the reactor
• Heat transfer medium preferably a metal bath
• a fluid to be evaporated or depolymerization material is supplied in the lower part.
• the high convection energies for heat transfer that occur in melting baths are able to store the stored energy in milliseconds for the fluid to be evaporated
• Metal baths are reduced to a minimum and, on the other hand, a better evaporation rate arises in the process, since the gas can distribute itself better.
• baffle plates are placed one behind the other in the steam flow direction, each of these baffle plates having a lateral opening and these openings being offset such that they do not in the steam flow direction
• the baffle plates can be arranged in the reactor space of the main reactor.
• a metal bath return can also be provided.
• the metal bath return is a component that was specially built for this application in order to collect small amounts of liquid metal in the reactor space above the metal bath surface and to feed it back to the reactor zone. Despite the steel balls, small amounts can still accumulate, which get caught in the metal bath return and back into the
• Reactor are recycled. The component ensures that gas can flow through but liquid metal gets caught and flows back into the actual metal bath.
• thermal energy is introduced into the waste oil by heat conduction, the excellent properties of the melting bath compensating for the temperature differences being used to achieve a
• a heat exchanger can be introduced into the reactor space of the main reactor, which has an inlet and an outlet, the inlet forming the inlet for the waste oil and its outlet in the inlet of the Rectification column opens.
• Gas bubbles can come in the weld pool.
• the heat exchanger can be designed as a tube, one side of which forms the entrance and the other side of which forms the exit. This tube can be wound in a spiral.
• the weld pool in particular a metal bath, surrounds the
• the melt pool ensures the even
• Fig. 2 is a schematic overview of a
• Fig. 3 a design of a main reactor for a
• Fig. 4 shows a design of a main reactor for a Countercurrent principle
• Fig. 5 the main reactor using the flow principle
• Fig. 6 the main reactor according to FIG. 4 with a
• Fig. 11 shows an arrangement of the metal bath return on
• Fig. 12 shows the arrangement of the metal bath return according to Fig. 10 with a metal bath filling and non-evaporated part
• Fig. 13 is a schematic diagram of the device in
• Fig. 15 is a schematic overview of a Device for cleaning contaminated waste oil according to the second embodiment
• Fig. 16 is a front view of an inventive
• Fig. 17 is a sectional view corresponding to the
• Fig. 18 is a cross-sectional view corresponding to the
• Line A A in FIGS. 17 and 19 is a plan view of the arrangement according to the invention of the second exemplary embodiment.
• the pipe T10 comes into direct contact with the heating gas generated by the combustion chamber TU.
• the heating gas is not evenly distributed on the temperature side in the tube furnace TI, so that the tube T10 partially overheats.
• the heat capacity of the heating gas is also low, so that high temperature differences have to be used, ie the heating gas is heated up strongly, which in turn can lead to overheating of the tube T10.
• slagging inside the tube T10 cannot be avoided, which is part of regular maintenance are remove. However, such maintenance prohibits the mobile use of such devices.
• contaminated waste oil is provided in an external input tank 1 for the purpose of cleaning by the device according to the invention shown in FIG. From this input tank 1, this waste oil is fed into an internal storage container 3 by means of a supply pump 2 and from there into the
• Main reactor 5 pumped.
• the amount of waste oil supplied is regulated as a controlled variable via the temperature in the rectification column 6.
• Depolymerization material 4 which is fed to the main reactor 5 and is suddenly evaporated therein by means of a so-called flash evaporation.
• exemplary embodiments produce steam which is fed to a rectification column 6. In this
• Rectification column condenses the steam in different stages, i.e. at different temperatures.
• Condensate on the first side drain 7 and the second Side draw 8, cooled via heat exchanger 11, are fed back to the template 3, the product, ie a cleaned oil is removed from the third side draw 9 and the top draw 10 and also cooled via heat exchanger 11, fed to a product tank 12. From there it is then fed into an output tank 14 by means of a product pump 13.
• Condensate which is not discharged via the fume hoods 7 to 10, and constituents of the depolymerization material 4, which do not evaporate and float in the metal bath of the main reactor 5, are returned to the main reactor 5 via a circulation line 31 by means of a circulation pump 32 for renewed evaporation as depolimerization material 4
• the condensate components that can no longer be distilled collect as a sump at the bottom of the
• a metal bath 19 which consists of a metal which has a melting point
• Depolymerization 4 has. The metal is kept in the liquid phase by heating sleeves 20. Since that
• Evaporation temperature must be, is evaporated immediately, as soon as it also enters the metal bath 19, one speaks of a flash evaporation.
• the design of the main reactor is shown in FIG. 3 and in FIG.
• De-polymerisation material 4 is fed directly to the underside of the metal bath 19 through the inlet 17 arranged directly on the underside of the main reactor 5 and evaporates there immediately.
• the undevaporated part 22 is mostly a higher-chain compound, which is largely due to the contamination of the waste oil in the
• Rectification can be supplied. As shown in Fig. 7, they relax
• a metal bath return 24 is arranged above the metal bath 19.
• This metal bath return 24 can be arranged, for example, in the reactor space of the main reactor 5 or in the rectification column 6. This metal bath return shows in
• Baffle plates 26 have a lateral opening 27, these openings being offset so that they are in
• the steam flow direction does not lie on top of each other, but covers each other.
• the baffle plates 26 can be clamped in the metal bath return 24 by means of a nut 28 which is screwed onto a pull rod 29.
• FIG. 12 shows the principle of the non-evaporated part flowing away as shown in FIG. 7, but with the metal bath return.
• the non-evaporated part 22 also floats on the metal bath 19, but fills the metal bath return 24 up to its upper edge. Since the undevaporated part 22 always experiences an increase, the excess flows over the upper edge of the metal bath return 24 into the sump container 15.
• the baffle plates 26 are located in the undevaporated part 22. The metal tips of the metal bath 19 thus reach within of the undevaporated part 22 to the baffle plates 26 and flow from there through the undevaporated part 22 back into the metal bath 19.
• a further measure for preventing the material discharge from the metal bath can consist in the fact that in the main reactor 5 packing 27
• packing elements can consist of a metal with a higher melting temperature than the metal bath 19 or other - possibly inert - materials, such as ceramic.
• Packing body 30 with a metal bath return 24, as shown in FIGS. 11 to 13, is possible.
• the effect can be seen in the fact that the vapor bubbles 23 which emerge from the inlet are still quite large and are broken up into smaller bubbles by the filling bodies 30. Steam bubbles 23 reduced in size in this way have only a lower energy when they burst on the surface of the metal bath 19,
• tin is used as metal for the metal bath 19 for the purpose of evaporating waste oil, since its melting temperature is
• Evaporation temperature of the depolymerization material is.
• the melting temperature must not be chosen so high that the
• Design of the device can be selected that works under vacuum. However, it is also possible to feed granulated plastics to a molten bath, preferably made of metal. The vapors escaping as a result of the heating can then be rectified to valuable raw materials. But also other heat transfer media, e.g. saturated salt solutions, melting plastics, and even liquid gases can be used in addition to the metals already described above as melt pool materials for a wide variety of applications.
• heat transfer media e.g. saturated salt solutions, melting plastics, and even liquid gases can be used in addition to the metals already described above as melt pool materials for a wide variety of applications.
• Prevention of combustion residues is also directed to the second exemplary embodiment, as is shown in FIGS. 14 to 19.
• Heating jackets 20 are arranged in the reactor vessel.
• the heaters can also be designed differently,
• induction heaters for example alternatively as induction heaters.
• Heating register 35 completely on. The heating register is thus washed around by the metal bath 19 when it is liquefied.
• the heating register consists of a spirally bent tube with a first end 38 and a second end 39.
• the cold waste oil is introduced into the first end 38 and led to the heating register 35 at its end facing the flange 36.
• the waste oil heated to the vapor phase enters at the second end 39 into that connected to it
• Device as a portable mobile
• Main reactors 5.1 to 5.4 and the type shown in FIG. 14 are provided, the second ends of which are each in the
• Rectification column 6 open, which is arranged centrally.
• a controller 41 is provided for the proper operation of the system.

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Engineering & Computer Science (AREA)
• General Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Physics & Mathematics (AREA)
• Thermal Sciences (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
• Separating Particles In Gases By Inertia (AREA)

Applications Claiming Priority (2)

Publications (1)

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• 2019
  • 2019-11-19 WO PCT/EP2019/081830 patent/WO2020104472A1/de not_active Ceased
  • 2019-11-19 JP JP2021527122A patent/JP2022507701A/ja active Pending
  • 2019-11-19 KR KR1020217018625A patent/KR20210102268A/ko not_active Ceased
  • 2019-11-19 CA CA3122117A patent/CA3122117A1/en not_active Abandoned
  • 2019-11-19 AU AU2019384362A patent/AU2019384362A1/en not_active Abandoned
  • 2019-11-19 US US17/294,569 patent/US20210402321A1/en not_active Abandoned
  • 2019-11-19 BR BR112021009471-7A patent/BR112021009471A2/pt not_active Application Discontinuation
  • 2019-11-19 SG SG11202105154QA patent/SG11202105154QA/en unknown
  • 2019-11-19 CN CN201980076492.3A patent/CN113195070A/zh active Pending
  • 2019-11-19 EP EP19817597.8A patent/EP3883661A1/de not_active Withdrawn

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