HUT67432A - Method and apparatus for regenerating waste oil and used oil-prducts - Google Patents

Abstract

Es wird ein Verfahren und eine Vorrichtung zum Regenerieren von Altöl oder dergleichen Stoffe vorgeschlagen, bei dem das Altöl in drei Reaktorstufen mit Hilfe von elektromagnetischer Strahlung ohne direkten Kontakt mit den Strahlungsquellen in drei Temperaturbereiche aufgeheizt wird. Dabei wird zur gezielten Strahlungszufuhr und zum Aufbrechen der Molekülketten von Schadstoffen das strömende Medium mehrfach an den Strahlungsquellen vorbeigeleitet.

Description

The present invention relates to a process and apparatus for the regeneration of waste oil and used oil products.

No. 32,429,298. In the US patent, a device is known for the recovery of waste oil from motor vehicles by the distillation of Krakow. The waste oil, after heating it on a preheater, is fed into a cracking tube containing a plurality of perpendicular infrared heating rods embedded in a quartz tube. The heating rods heat up the waste oil flowing through them, which is cracked. The higher boiling components evolve gases and vapors which are fed into a fractionator to extract gasoline and diesel. This device is advantageous if it can be constructed in a relatively small size and the heating rods, due to their incorporation in the quartz tube, do not come into direct contact with the waste oil and thus coke. However, experience has shown that this equipment is not working properly and cannot be implemented in practice.

It is an object of the present invention to provide a process and apparatus for the recovery of waste oil which allows the waste oil to be regenerated in a simple and satisfactory manner, whereby the harmful substances contained therein can be completely removed.

It has been found that this object can be achieved by a process in which the material to be regenerated is to be used. · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · and heating to a different temperature depending on the composition of the medium.

The process according to the invention is preferably carried out as follows.

The radiation energy and / or the spectra of the electromagnetic radiation source are adjusted according to the bonding energy between the atoms of the medium and / or the optimum radiation depth of the medium.

The medium is fed to the electromagnetic radiation source in stages in at least one reactor stage and is discharged from the electromagnetic radiation source.

The operations of the process are preferably carried out in an oxygen-free or at least oxygen-deprived environment, in a protective gas atmosphere or optionally under slight pressure.

It is expedient to rinse the equipment used for the process with an antifouling and anti-coking agent before starting.

The materials degassed from the third reactor stage are fed to a heat exchanger, the high boiling components are condensed and recycled to the third reactor stage.

• · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · current were were principal general general position;

The flux medium is preferably irradiated with IR and / or UV rays.

The process described above can advantageously be carried out in an apparatus according to the invention having two, preferably three in series, reactors 3, 4, 5, in which the spent oil is heated to different temperature ranges 13 before the waste oil is recirculated and a plurality of drain guides 14, 15, and a heat exchanger separator coupled thereto to the reactors.

The apparatus according to the invention is preferably configured as follows.

The radiation sources 13 are elongated and are arranged one after the other in the reactors 3, 4, 5 transverse to the flow direction. The number in each reactor is selected according to the desired temperature range.

The reactors 3, 4, 5 have vertically arranged flow reversing guide plates 14 as well as inverting and settling structures 15 which facilitate the separation of solids from the flow medium at the bottom of the reactors.

In the evaporation zone e1 of the reactors 3, 4, 5, elements for preventing the discharge of solids and liquids are incorporated.

• · ti »ί» · • «« * * * * * * * «« «« «« ««

Above the third reactor 5 is a heat exchanger with an adjustable temperature setting forming an integral part thereof, from which the non-cracked products flow directly back to the third reactor.

A static mixer 35 having at least one high energy source 21, preferably a UV source, is provided between the at least two reactors and has diverting means 22 for feeding the waste oil to and from the source.

Optionally, the radiation sources 13 of the device are flat and are set at different angles to the flow direction.

Finally, it may be advantageous for practical application if the device is designed as a compact, optionally mobile module.

An important advantage of the device according to the invention is that it can be set up as a compact and optionally mobile device near the place where the waste oil is produced and suitable for the purpose of processing waste oils in smaller quantities. Since the equipment is usually operated in conjunction with a particular plant or company, which produces uniform waste oil, the process or equipment parameters can be adjusted to the quality of the previously analyzed waste oil. The final product leaving the equipment • · · ················································

6 can advantageously be used as a fuel in a heat recovery unit. The fact that three reactors at different temperatures are connected in series and thus the energy input is distributed between several reactors allows for specific temperature differences to be adapted to the different sources of waste oil material.

As a result, we operate the unit practically free of overpressure. Due to the construction of the reactors, the flow continuously surrounds the radiation sources and thus a homogeneous treatment of the medium is ensured with a low irradiation depth. The irradiation energy can be coordinated with the bonding energy of the atoms when using both IR and UV rays and other radiation spectra. Thus, it is possible to provide for the decomposition of the molecules of harmful substances into harmless substances when processing waste oils containing harmful substances. The energy required for cracking is introduced not only in the form of heat radiation, but simultaneously in the form of energy radiation, whereby the molecular chains reach their own frequency for their breaking up. Due to the target energy supply that causes increased molecular movement1, the molecules of the harmful substances explode without excessively raising the temperature of the waste oil to be regenerated, and the resulting radicals are the product of past reactions. · · »* ·«! ·· »» · * · »··» 9 · * · ·· · »

- Reacts with 7 carbon atoms or with free hydrogen atoms to become harmless substances.

The guide plates divide the reactor into an energy supply zone and a fluid return zone. This ensures a high-speed forced flow of the fluid flowing around the radiation sources and the fluid flowing outside the guide plates. Specially designed turning and settling structures create relaxation zones in the lower part of the reactors. These can continuously remove materials that are no longer needed to continue the process. Advantageously, additional structural elements incorporated in the steaming zones prevent the discharge of liquid or solid materials, such as soot particles or high boiling liquid materials, that impair the quality of the product. The temperature profile necessarily resulting from the structure of the reactor provides a high velocity flow along the reactor cross-section. This effect, as well as the injection of energy for the reaction through radiation sources, prevents coking and other substances from settling in the equipment. The deposition of materials in the equipment may be further prevented by impregnating the equipment or parts thereof with suitable materials such as special amines.

Preferably, the first heat exchanger and the last reactor form one unit. In this way, a self-regulating forced-return rate is established. The reactor heat exchanger is designed to re-design non-cracked products. * "• · · · · '····" ·· ······ »· _a *

- We recycle it 8 times and react again. After adjusting the temperature of the first heat exchanger, the width of the product fraction at the upper boiling point is adjusted to the requirements. After the reactors, one or more boiling point fractions can be recovered from the product stream by means of coupled heat exchangers.

The invention is illustrated by the examples shown in the drawings, the details of which are set forth below. The

Figure 1 is a flow diagram of an apparatus according to the invention, a

Figure 2 is a schematic drawing of a reactor, a

Figure 3 is a sectional view of a reactor according to the invention at the height of a radiation source, a

Fig. 4 is a flowchart of another embodiment of the apparatus of the present invention

Figure 5 is a sectional, side and top view of a static mixer according to the invention.

In the process of Figure 1, used oil, such as used lubricating oil for various internal combustion engines, speed, and other similar used oil products, is collected by a collector 1, to which the oil is pumped from the user. In front of or parallel to this, a separator 2 is connected for mechanical pre-cleaning. The collection vessel 1 is connected to the first reactor 3 by means of a pump 12 to which a second reactor 4 and a third reactor 5 are connected in series 9. . The reactors 3, 4, and 5, as illustrated in more detail in Figures 2 and 3, have radiation sources 13 transverse to the reactor axis, i.e. perpendicular to the flow direction of the fluid flowing through the reactor and introduced into the reactor from outside through seals. The radiation sources 13 are closed from the outside with a quartz tube. The quartz tube may have a shape other than that shown in the figure, such as flat or oval. In this case, the radiation sources 13 are set at different angles at different heights of the reactors relative to the flow direction. The radiation sources 13 are IR radiation sources, but they may also be radiation sources of different spectrum. Optionally, at least part of the zones may also be provided with UV radiation. The reactors 3, 4 and 5 have different number of radiation sources 13, for example 3 in reactor 3, 5 in reactor 4 and 7 in reactor 5.

As shown in Figures 2 and 3, vertical guide plates 14 are provided on each side of the radiation sources 13 in each reactor. These reactors are divided, for a substantial part of the length of the reactor, into an energy supply zone surrounding the radiation sources and a fluid recirculation zone. These guide plates 14 ensure a continuous flow, which is set based on the temperature differences in the reactors.

In the lower part of the reactors there are turning and settling structures which form a rest zone. These are • · • · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · ·–– detail room detail

- 10 reverses the flow and separates solids that have not been removed from the medium during mechanical pre-cleaning or in pre-filtration stages not shown in the figures.

In the upper part of the reactors, in the evaporation zone, there are separating elements 36, on which the vapor-entrained liquid and solid materials can be separated and recycled to the flow medium.

The structure of reactors 3, 4 and 5 is theoretically the same except for the number of radiation sources.

The spent oil pumped from the collection tank into the reactor 3 is heated with the jet sources 13 to 80-180 ° C, preferably 90-110 ° C, while being repeatedly turned in the direction of the arrows shown in Fig. 2 and drained several times before the jet sources. During this time, water and solvents, i.e., volatile components, are removed in the form of a gas, which is conveyed through a conduit and an intermediate container 37 to a collecting vessel 38 provided with a heat exchanger 39.

Several times, after digging, a portion of the fluid flows out of reactor 3 and flows into reactor 4, where several radiation sources 13 heat to a higher temperature of 180-350 ° C. The medium also flows through the reactor 4 several times before the radiation sources. The temperature of the reactor 4 allows the gasoline and diesel fractions in the waste oil to be vaporized. These are fed into the heat exchanger 40.

The heat exchanger 40 is disposed above the reactor 5 and forms a unit therewith. In Reactor 5, the radiation in the reactor.

By gentle yet direct injection of 11 energy, cracking occurs at temperatures of from 400 to 450 ° C, with the fluid flowing back into the heat exchanger 40 again. The head temperature, which is adjustable, is about 350-380 ° C. Due to the arrangement of the third reactor 5 and the heat exchanger 40, a self-regulating forced-reflux ratio is set and the desired boiling range of the fraction can be determined.

The diesel and gasoline fraction mixture leaving the heat exchanger 40 is fed to a collection vessel 41 for collecting gasoline and diesel fractions, which is connected to a heat exchanger 42 having a head temperature of 40 ° C. In the latter, the gasoline-diesel fraction condenses. The collecting container 41 is connected to a collecting container 43 for collecting a mixture of petrol and diesel fractions, which is then connected to the intermediate container 37 as well. In the heat exchanger 39 and the collecting vessel 38, a mixture of water, gases and other substances is formed. The gases may be discharged by means of a vacuum pump or an overflow valve.

The hopper 44 receives an emulsion of the residual material.

Of course, the gasoline and diesel fractions leaving the heat exchanger 40 can be further fractionated beyond the operations shown in Figure 1, but the mixed fraction itself can be used for many purposes.

The temperature of reactors 3, 4 and 5 is adjustable depending on the composition of the medium and is limited by the combined control of material flow and radiative power. · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · Thus, the radiation power can also be controlled depending on the material composition of the medium, and the radiation frequency can also be adjusted according to the medium. The combination achieves high efficiency in terms of energy input at low temperatures. The three reactors, namely, 3, 4 and 5 of the reactor feed stream is controlled in accordance with the charging state, such as _x natural drop develops. The apparatus shown in Figure 1 is operated at a slight overpressure of about 30-60 mbar to prevent oxygen from entering the apparatus.

The separator 2 helps to prevent sedimentation and carbonation. The optimum separation temperature of the mechanical device can be achieved by utilizing the waste heat of the device. Some or all of the aqueous phase may also be separated from the separator.

Optionally, for example, in the case of a suitable composition of the waste oil or in the processing of a low-contaminated waste oil, the second or third reactor may be omitted by adjusting the process parameters to the particular configuration.

Figure 4 shows an apparatus similar to that illustrated in Figure 1, which can be used to process particularly contaminated waste oils and to obtain multiple boiling range. In the figure, like or corresponding parts of the apparatus of Figure 1 are denoted by like numerals.

· · * * • · · ·

To reactors 3, 4 and 5 corresponding to the reactors of the same designation in Figure 1, capacitors 9, 10 and 11, respectively, are connected, in which easily volatile materials are condensed and can be of several stages. Three condensation stages are connected to the three reactor stages, namely the residue condenser 6, the diesel condenser 7 and the gasoline capacitor 8.

The second reactor of Figure 4 differs therein from Figure 1

X second reactor to a temperature of 180-250 ° C. Thus, residual solvent water residues in the fluid flowing therein are removed by evaporation and optionally separated in the condenser 10.

A static mixer is inserted between the first reactor 3 and the second reactor 4, which is illustrated in more detail in FIG. The mixer consists of a plurality of parallel-placed pipes 18 which open at the common inlet 19 and their outlets at the common outlet 20.

The tubes 18 are provided with longitudinally extending radiation sources 21. The distance between the radiation source 21 and the wall of the tube 18 is adapted to the depth of radiation penetration.

The radiation sources 21 are surrounded by deflectors 22 which, in stages, guide the flowing waste oil or its particles into and out of the radiation source 21. The tubes 18 are surrounded by a housing 23 having an inlet 24 and an outlet 25 for coolant. Coolant flows around the pipes in this way.

··· · · · · · · · · · · · · · · · · · · · · ··· ·

- 14 In the static mixer, the molecules are supplied with energy to break up the molecular chains of the harmful substances in the waste oil, which is necessary for them to reach their self-frequency. In order not to overheat the waste oil as a whole, the baffles 22 are used to guide the particles into the active zone of the radiation sources 21 for the desired energy uptake and then from there. If necessary, heat can be removed from the coolant flowing into the housing 23. The radiation spectrum of the radiation sources 21, like other radiation sources, can be adjusted according to the harmful substances to be decomposed. It is desirable to use high-energy radiation, such as UV radiation.

The gas obtained by evaporation in the third reactor 5 is passed through the condenser 11 of the volatile materials into the residual condenser 6 to which the diesel condenser and the gasoline condenser are connected. The three capacitors, i.e. capacitors 6, 7 and 8, are controlled at different temperatures, respectively 360 ° C, 200 ° C and 40 ° C. In the residual condenser, all high-boiling point components, such as tar and paraffins, condense above 360 ° C and return to reactor 5 via line 28 for re-cracking there.

At the bottom of the reactor 5, bitumen accumulates and is conveyed by the conveyor screw 29 to the bitumen collecting tank 30. Preferably, however, the bitumen can also be irradiated with a UV beam and recirculated into a circular stream;

• · · · »· · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · draft ·

- 15 matba.

In the Diesel condenser 7, the components that condense in the range of 200-360 ° C are separated. These form the diesel oil which is passed through the oil cooler 31 to the diesel tank 32.

Substances remaining in gaseous form after the diesel condenser 7 are separated in the gas condenser 8.

These form the petrol which is collected in the tank 33. A small amount of gas leaving the gasoline condenser 8 is fed to the gas line 17 and optionally, after further separation, is flared or otherwise used. The water leaving the diesel condenser and the gas condenser is collected in the 34 water tanks.

Optionally, a hydrogen source 45 may be provided to supply the third reactor 5 with hydrogen, but hydrogen may be introduced into the other reactors.

In the example shown, the static mixer 35 is disposed between the first reactor 3 and the second reactor 4, but instead or additionally, a static mixer can be arranged between the second reactor 4 and the third reactor 5. Such a device can also be used for pre-treatment of waste oil and post-treatment of the resulting product.

Because of the high efficiency of the apparatus shown in Figure 1 and Figure 4, it can be configured in a module and thus set up at the site of the potential customer. In addition, the recovered fuel can be used, for example, to operate an aggregate that supplies electric power to the unit. · · · · · · · · · · · · · Pumps, radiation sources and other units of the equipment. It may also be advantageous to combine the unit with a block thermal power plant. The waste heat of the unit can be combined with the energy required for operation.

Non-energetically recoverable gases leaving the first reactor and materials leaving the separation unit at about 30 ° C in a gaseous form are purified or thermally purified by an activated carbon filtration system.

Claims (15)

Claims A process for the regeneration of waste oil and used petroleum products, characterized in that the material to be regenerated is passed through at least two reactor stages, preferably three in series, into a reactor stage, and heating to a different temperature depending on the composition of the medium. Method according to Claim 1, characterized in that the radiation energy and / or the spectra of the electromagnetic radiation source are adjusted according to the binding energy between the atoms of the medium and / or the optimum radiation depth of the medium. Method according to claim 1 or 2, characterized in that the medium is introduced in stages in at least one reactor stage into the electromagnetic radiation source and is discharged from the electromagnetic radiation source. 4. A process according to any one of claims 1 to 3, characterized in that the operations are carried out in an oxygen-free and / or oxygen-deprived environment, in a protective gas atmosphere and / or under slight pressure. 5. The method according to any one of claims 1 to 5, characterized in that the apparatus used for the method ·· ·· · - Prior to start-up, flushing with 18 anti-caking and anti-coking agents. 6. A process according to any one of claims 1 to 3, wherein the material degassed from the third reactor stage is fed to a heat exchanger, the high boiling components are condensed and recycled to the third reactor stage. 7. A method according to any one of claims 1 to 3, characterized in that the flow medium is irradiated with IR and / or UV rays. Apparatus for regeneration of waste oil and used petroleum products, characterized in that it has two, preferably three in series reactors (3, 4, 5), electromagnetic radiation sources (13) for heating the waste oil in different temperature ranges and several times the waste oil there are guides (14, 15) for reversing and repeatedly discharging in front of the radiation sources, and a heat exchanger / selector coupled thereto to the reactors. Apparatus according to claim 8, characterized in that the radiation sources (13) are elongated and are arranged one after the other in the reactors (3, 4, 5) transverse to the direction of the milling and in the individual reactors (3, 4, 5). ) according to the desired temperature range. The apparatus according to claim 8 or 9, characterized in that the reactors (3, 4, 5) - 19 flow-reversing baffles (14) and rotating and settling structures (15) located on the underside of the reactors to facilitate separation of solids from the fluid. 11. Apparatus according to any one of claims 1 to 4, characterized in that the evaporation zone of the reactors (3, 4, 5) comprises elements preventing the discharge of solid and liquid substances. 12. A 8-11. Apparatus according to any one of claims 1 to 5, characterized in that an adjustable temperature-adjustable heat exchanger is disposed above the third reactor (5), from which the products not yet cracked are returned directly to the third reactor. 13. A 8-12. Apparatus according to any one of claims 1 to 4, characterized in that between at least two reactors there is a static mixer (35) having at least one high energy radiation source (21), preferably a UV radiation source, (22) are. 14. A 8-13. Apparatus according to any one of claims 1 to 3, characterized in that the radiation sources (13) are flat and are arranged at different angles to the flow direction. 15. A 8-14. A device according to any one of claims 1 to 4 sorting, characterized by compact, case- ben is designed as a mobile module. THE ·. ADVOT ATENT FREE ADAJ Ml OFFICE. CHRISTMAS BÉLA mailing address; 1251 Bp. Pf. 11. i