EP3883661A1

EP3883661A1 - Method and device for cleaning contaminated used oil

Info

Publication number: EP3883661A1
Application number: EP19817597.8A
Authority: EP
Inventors: Michael Richter
Original assignee: Biofabrik Hoyerswerda GmbH
Current assignee: Biofabrik Hoyerswerda GmbH
Priority date: 2018-11-19
Filing date: 2019-11-19
Publication date: 2021-09-29
Also published as: JP2022507701A; US20210402321A1; BR112021009471A2; KR20210102268A; CA3122117A1; CN113195070A; WO2020104472A1; SG11202105154QA; AU2019384362A1

Abstract

The invention relates to a method and a device for cleaning contaminated used oil, in which starting material is heated to the gas phase and the resultant vapour is rectified, with purified oil being removed as condensate from a drain in a rectification column. The problem addressed by the invention is that of providing a method and device for purifying contaminated used oil, which method enables efficient operation even in the smallest of systems, such that a compact system configuration and thus in particular mobile use by a container structure is made possible. The invention also addresses the problem of reducing the cost required for servicing. The problem according to the invention is solved in that used oil is subjected to an evaporation process by at least indirectly placing the starting material in contact with a melting bath, the melting temperature of which is above the evaporation temperature but below the ignition temperature of the used oil, and by rectifying the vapour in the rectification column.

Description

Method and device for cleaning dirty

Waste oil The invention relates to the processing of

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

Starting material is used in the process. The

The waste oil can be cleaned by pure distillation without changing the molecular structures. The

However, the invention can also be used in a temperature range

are used in which so-called cracking takes place, i.e. breaking up long molecular chains into shorter ones. The invention relates to a method for cleaning contaminated waste oil, in the starting material up to

Gaseous phase warmed and the resulting steam

is rectified, with purified oil being removed as condensate from a fume cupboard in a rectification column. 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 process of cracking and the subsequent distillation is known from the heavy or crude oil industry and

described for example in www.seilnacht.com/versuche/erdoeld.gif and shown again in Fig. 1. The crude oil is heated to over 360 ° C in a tube furnace so that the components largely evaporate. These reach a distillation tower, which is made up of numerous bell bottoms. The distillates of the individual fractions collect in the bell bottoms. The temperatures of the bell bottoms decrease upwards. The rising steam then condenses in each bell bottom, the temperature of which is below the boiling point of a component, that component. The individual components can thus be separated.

In the tube furnace, the starting material comes into contact with a hot gas via a heat exchanger. To

it is sufficient heating of the starting material

necessary to choose such a temperature difference that allows heating up to the target temperature. This means that the inner tube of the heat exchanger tends to clog, as there are combustion residues on the inside. The outside is also exposed to heavy loads from the heating gas. This does not create a

insignificant maintenance effort. This is not a problem in large stationary plants, since there are several reactors

can be used so that one or more are always available for operation, even if others need to be serviced. Such redundancy is not possible in smaller and mobile systems, at least disadvantageous.

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

Liquid phase and due to the delayed penetration of the filler into the vapor phase and is in one

Condenser condensed to an output material and collected in a collector. 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.

Treatment of waste oil as a starting material with a metal bath is not known from the sources mentioned.

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

reduce .

In the process according to the invention, contaminated oily residues are automatically cleaned, condensed and thus usable again within a few minutes

Fuel is transformed. The process can use known processes from the crude oil industry with a depolymerization process designed according to the invention

combine hydrocarbonaceous raw materials and so-called cold cracking technologies.

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

The influence of temperature is released again and products of shorter chain lengths are created, e.g. again oils (medium length), but also waxes (somewhat longer chains, also liquid when heated), and gases (very short chains), all of which are well suited for energy use, in the case of oils also excellent for storage and transport. These can also be used as the starting material for the

inventive method are used.

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

Melting temperature above the evaporation temperature but below the ignition temperature of the waste oil is subjected and the steam is rectified in the rectification column.

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.

In one embodiment of the method according to the invention it is provided that 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. Through this

Thermal conduction evaporation ensures a uniform

Energy amount in the waste oil, which is a slagging of the

Avoids heat exchanger surfaces and at least thereby significantly reduces the maintenance effort.

Common to the designs of the method according to the invention is the use of a melting bath. It is possible that liquid metal is used as the molten pool. It is possible that tin or lead is used as the metal.

In every design, the gas phase is processed in a special rectification process separated into pre-defined and controlled fractions from heavy to low boilers. So arise

different qualities of distillate. Engine-compatible fuels are removed, unclean fractions can

Repeat the process until they are completely separated into usable and waste components. The various oil fractions continue to expand depending on the area of application

refined or in the form of finished products

Distributors or end customers shipped. In the waste discharge 5 to 10 percent of the raw material falls as tar-like

Waste. This can be used for bitumen production in road construction or as a substitute fuel. There is no further waste. The use of the rectification process in the small plant area combined with one

Melting pool evaporation is the focus of the invention.

It is also possible for an onboard generator to supply the device with energy from self-produced fuel or from a residual gas. Such a device then works self-sufficient in terms of energy. In this way, an overall efficiency of approx. 75% percent is currently achieved. Each unit processes up to 1,000 liters of raw material daily - however, this can be modular to an unlimited size

Raw material quantity to be expanded.

On the device side, 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

Melting pool material, the melting temperature of which

Evaporation temperature, however, is below the ignition temperature of the waste oil, the reactor chamber is filled with a

Heating device is provided and an inlet in the reactor is arranged for the waste oil.

In one embodiment of the device according to the invention, 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

Melting pool is formed.

In a reactor tube, which as the melt pool

Heat transfer medium, preferably a metal bath, is filled and is vertical or arranged obliquely, 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

feed.

When using melt baths as a heat transfer medium, however, there can be uncontrolled explosions, which can lead to a loss of the heat transfer medium. This process step creates very large gas bubbles, which relax / burst on the surface. As a result, part of the metal bath is entrained and collects in the reactor sump or places lines or the like. If this effect is taken for granted, the result is that the process is interrupted after defined operating times and the original bath has to be added to the metal bath at great expense. The object of the invention is achieved by

Avoiding the interruption of operating hours. For this purpose, the metal bath losses occurring in continuous operation are counteracted in melt pool reactors. For this purpose it can be provided that at

Convection reaction to large gas bubbles

reduce in order to minimize the entrainment of the metal bath when these gas bubbles relax. It is possible to fill the reactor zone with fillers such as

Fill steel balls so that the gas bubbles at the

Penetration of the reactor zone then occur quickly and arrive in small bubbles on the surface of the metal bath. With the help of these filling materials, you have two main ones

Benefits created. On the one hand, the entrainment of the

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.

In a further embodiment of the device

provided to ensure a metal bath return by means of baffle plates, whereby metal bath splashes directly into the

Metal bath can be recycled. For this purpose, 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

lie on top of each other, but cover each other.

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.

Another solution can be chosen to avoid melt pool losses. This provides for an indirect heat-conducting connection in the reactor space

is provided between the waste oil and the melt pool by a partition between the waste oil and the melt pool

is provided, through which the waste oil is separated from the molten bath.

Due to the heat-conducting connection, 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

To cause evaporation without slag or similar phenomena occurring on the heat-conducting connection, as is the case, for example, with the known tube furnaces.

For implementation, 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.

With such a heat exchanger, a highly efficient and even energy input into the waste oil is achieved without causing melt pool losses as a result of bursting

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

Heat exchanger. The melt pool ensures the even

Energy input, because newly fed used oil must first be warmed up. The large heat capacity of the melting bath allows the waste oil to be heated up quickly, without causing a significant drop in the temperature of the melting bath or slagging during the energy input.

The invention is described below with reference to a first

Embodiment (Fig. 2 to 13) and a second embodiment (Fig. 14 to 17) described in more detail. 1 shows an illustration of the prior art,

Fig. 2 is a schematic overview of a

Device for cleaning contaminated waste oil according to a first embodiment,

Fig. 3 a design of a main reactor for a

Continuous flow principle,

Fig. 4 shows a design of a main reactor for a Countercurrent principle,

Fig. 5 the main reactor using the flow principle

Filling elements,

Fig. 6 the main reactor according to FIG. 4 with a

Bubble distribution of the depolymerization material,

Fig. 7, the main reactor in the countercurrent principle with a

Bubble distribution of the depolymerization material,

Fig. 8 with the main reactor in the countercurrent principle

Filling elements and bubble distribution of the depolymerization material,

9 is a schematic diagram of a metal bath return in plan view,

10 shows the metal bath return in cross section,

Fig. 11 shows an arrangement of the metal bath return on

Main reactor

Fig. 12 shows the arrangement of the metal bath return according to Fig. 10 with a metal bath filling and non-evaporated part and

Fig. 13 is a schematic diagram of the device in

cross-section

14 shows a main reactor according to the heat conduction evaporation principle according to a second exemplary embodiment,

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

Device according to the second

Embodiment

Fig. 17 is a sectional view corresponding to the

Section line B - B in Fig. 16,

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.

As shown in Fig. 1, according to the prior art in the tube furnace TI, the crude oil is heated to over 360 ° C, so that the components largely evaporate. These reach the distillation tower T2, which consists of numerous

Bell bases T3 is built. The distillates T4 to T9 of the individual collect in the bell bottoms T3

Fractions. As can be seen, the pipe T10, in which the waste oil is guided, 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. As a result, 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.

According to a first embodiment of the invention, 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.

Before the added new waste oil enters the main reactor 5, the waste oil mixes with the following

described distillate and bottom refluxes to one

Depolymerization material 4 which is fed to the main reactor 5 and is suddenly evaporated therein by means of a so-called flash evaporation.

It should already be mentioned here that the same basic run as shown in FIG. 2 also applies to the second exemplary embodiment. The main difference is in the main reactor. The main reactor in the second exemplary embodiment does not perform flash evaporation but instead conduction evaporation. In both

However, 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. On this

Levels 7 to 10 are provided. During that

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

fed.

The condensate components that can no longer be distilled collect as a sump at the bottom of the

Rectification column. From there, the sump is fed to the disposal container 15 via a sump return 16. From there, the content of the

Disposal container 15 in an external disposal tank As shown in Fig. 3, the main reactor 5 can be carried out on the continuous principle. At the lower end there is the entrance 17 for the

Depolymerization material 4 and at the upper end of the outlet 18. In the main reactor 5 there is a metal bath 19, which consists of a metal which has a melting point

above the evaporation temperature of the

Depolymerization 4 has. The metal is kept in the liquid phase by heating sleeves 20. Since that

Depolymerization material 4 by the temperature of the metal bath 19, which is in the liquid phase above the

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.

4 shows two variants. Fig. 3

represents the flow principle, in which the

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.

4 represents the counterflow principle, in which the inlet 17 has a counterflow tube 21. The depolymerization material 4 is guided through the metal bath 19 through this counterflow tube 21. This warms up

Depolymerization material 4 already up to almost

Evaporation temperature, so that the flash evaporation takes place even faster when it exits the inlet 17.

As shown in Fig. 7, parts of the

Depolymerization 4 by the temperature of the

Metal bath 19 not evaporated. The undevaporated part 22 is mostly a higher-chain compound, which is largely due to the contamination of the waste oil in the

Inputtank come. As can be seen from FIG. 7, this part 22 floats on the metal bath 19 and flows at the connecting edge between the main reactor 5 and

Rectification column in the sump container 15. This, together with the rest of the sump, can be replaced

Rectification can be supplied. As shown in Fig. 7, they relax

resulting vapor bubbles 23 on the surface of the

Metal bath 19 and burst. In order to prevent 23 parts of the metal bath 19 from being entrained during the expansion of the vapor bubbles, which in the end would then

Sump container 15 land or clog lines and what minimizes the fill level of the metal bath 19, 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 lying on the steam flow direction 25, as shown in FIGS. 8 to 12. Any of these

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.

If metal drops are now emitted from the metal bath 19 and carried along by the steam flow, they hit one of these baffle plates 25 and flow back into the metal bath 19 from there.

In order to ensure that the metal of the metal bath 19 does not condense on the baffle plates 26, these should be one

Have temperature above the melting temperature of the metal bath 19. This can be ensured by heat conduction via the wall of the main reactor 5 and, in the event that the baffle plates are arranged in the rectification column 6, via the wall thereof. In not shown It is also possible to heat the baffle plates 25.

FIG. 12 shows the principle of the non-evaporated part flowing away as shown in FIG. 7, but with the metal bath return. Here, 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. As can be seen here, 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.

As shown in FIG. 5, 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

be introduced. These 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.

Such a filling with packing elements 30 is possible both in the continuous flow principle according to FIG. 3, shown in FIGS. 5 and 6 and in the countercurrent principle according to FIG. 4, shown in FIGS. 7 and 8. Also a combination of the

Packing body 30 with a metal bath return 24, as shown in FIGS. 11 to 13, is possible. As shown in FIG. 6 and FIG. 8, 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,

To emit metal splashes.

In the exemplary embodiment described above, tin is used as metal for the metal bath 19 for the purpose of evaporating waste oil, since its melting temperature is

300 ° C optimally matches the evaporation temperature of the used oil.

However, it is also possible to use other metals. The use of other melting materials is also possible. The only important thing is that the melting temperature of the melting material used is equal to or greater than that

Evaporation temperature of the depolymerization material is. However, the melting temperature must not be chosen so high that the

Depolymerization goods, not even partially. Incidentally, this is the advantage of the metal bath or, more generally, the melt pool solution. If the depolymerization material is used directly, i.e. without one

Weld pool, e.g. heated by external heat energy input through the wall of the main reactor, the temperature gradient inevitably leads to

Overheating of the depolymerization material on the wall and thus for the deposition of combustion residues, which soon leads to complex cleaning of the main reactor

be required. This also shows other areas of application for the molten bath solution. For example, it becomes possible to use contaminated solvents or cleaning agents

Process fuels. Then one in particular

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.

On preventing melt pool loss and one

Prevention of combustion residues is also directed to the second exemplary embodiment, as is shown in FIGS. 14 to 19.

14 shows a main reactor 5 which has a reactor vessel 34. On the outside of the

Heating jackets 20 are arranged in the reactor vessel. The heaters can also be designed differently,

for example alternatively as induction heaters.

This is inside the reactor vessel 34

Metal bath 19. A heat exchanger or

Heating register 35 completely on. The heating register is thus washed around by the metal bath 19 when it is liquefied.

At the top is the reactor vessel 34 with a

Provided flange 36, by means of which the reactor vessel 34th can be connected to the main reactor 5. A drain hole 37 is provided in this flange 36, through which non-condensable liquid can be drained directly into the sump. 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

Rectification column 6. There is already

described distillation instead.

15 shows the principle that the waste oil heated to the vapor phase is fed to the rectification column 6 via the second end 39 and evaporates therein. The fractions of the waste oil that are not yet properly condensed in the rectification column 6 are fed into the main reactor together with new waste oil as depolymerization material 4 at its first end 38 to the heating register 35. 16 to 19 show that the

Device according to the invention as a portable mobile

Device is arranged in a frame 40. In this

are the storage container 3, the product tank 12 and the disposal container 15. There are four to increase the production capacity

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.

Method and device for cleaning dirty

Waste oil

Reference symbol list

1 input tank

2 master pump

3 storage containers

4 depolymerization material

5 main reactor

5.1 - 5.4 main reactor

6 rectification column

7 first side print

8 second side deduction

9 third side trigger

10 head trigger

11 heat exchangers

12 product tank

13 Product pump

14 output tank

15 disposal containers

16 sump return

17 admission

18 exit

19 metal bath

20 heating jackets

21 counterflow tube

22 unevaporated part

23 vapor bubbles

24 metal bath return 25 Steam flow direction

26 baffle plate

27 side opening

28 mother

29 tie rod

30 packing

31 Circulation line

32 circulation pump

33 disposal tank

34 reactor vessels

35 heat exchangers, heating registers

36 flange

37 drain hole

38 first end

39 second end

40 frames

41 control

Claims

Method and device for cleaning contaminated waste oil

1.Process for the purification of contaminated waste oil, in which the starting material is heated up to the gas phase and the resulting steam is rectified, whereby purified oil is removed as condensate from a discharge in a rectification column, so that the waste oil is considered as

Starting material used and evaporation by at least indirect contacting the

Starting material is subjected to a melt pool (19), the melting temperature of which is above the evaporation temperature but below the ignition temperature of the waste oil, and the steam in the

Rectification column (6) is rectified.

2. The method according to claim 1, d a d u r c h

It is a fact that flash evaporation is carried out using the raw material

Melting bath (19) is fed directly.

3. The method according to claim 1, d a d u r c h

characterized in that the starting material is fed indirectly to the melt pool (19) by passing it through the melt pool (19) without a direct connection and via a heat-conducting connection.

4. The method according to claim 1, wherein the metal bath is used as the molten pool (19).

5. The method according to claim 4, d a d u r c h

It is important that tin or lead is used as the metal.

6. The method according to any one of claims 1 to 5, that a condensate is fed to a new rectification.

7. Device for cleaning contaminated waste oil with a main reactor (5) and a rectification column (6) connected to it, d a d u r c h

it is that the main reactor (5) is designed as a molten bath evaporator by adding a reactor space (34) with a molten bath material (19), the melting temperature of which is above the

However, the evaporation temperature is below the ignition temperature of the waste oil, is filled, the reactor space (34) is provided with a heating device (20) and an inlet (17) for the waste oil is arranged in the reactor (5).

8. The device according to claim 9, d a d u r c h

characterized in that a direct heat-conducting connection between the waste oil and the molten bath (19) is realized in the reactor space by the entry (17) into the reactor (5) directly into the Melting pool (19) is formed.

9. The device according to claim 8, d a d u r c h

g e k e n n e i c h n t that above the

Melting bath (19) in the steam flow direction (24)

baffle plates (25) lying one behind the other are introduced, each of these baffle plates (25) being one

has lateral opening (26), these openings being offset such that they do not lie one above the other in the steam flow direction, but rather cover one another.

10. The device according to claim 8, d a d u r c h

it is that the baffle plates are arranged in the reactor space of the main reactor (5).

11. The device according to claim 9, d a d u r c h

it is that an indirect heat-conducting connection between the waste oil and the melt pool (19) is provided in the reactor space (34) by providing a partition between the waste oil and the melt pool (19) through which the waste oil is removed from the

Melting pool (19) is separated.

12. The apparatus of claim 11, d a d u r c h

it is that a heat exchanger (35) is in the reactor chamber (34) of the main reactor (5)

is introduced, which has an entrance and an exit, the entrance forms the entrance for the waste oil and its exit in the entrance of the

Rectification column (6) opens.

13. The apparatus of claim 12, d a d u r c h

It is ensured that the inlet on the side facing the rectification column (6) and the outlet on the side of the main reactor (5) facing away from the rectification column is arranged.

14. The apparatus of claim 13, d a d u r c h

it is that the heat exchanger (35) is designed as a tube, one side (38) of which forms the entrance and the other side (39) of which forms the exit.

15. The apparatus of claim 13 or 14, d a d u r c h g e k e n n z e i c h n e t that the tube is wound spirally.