Plant and process for the catalytic production of diesel oils from organic materials

Abstract

Plant (1) for the catalytic production of diesel oil (9) from a feedstock (7) from the group of residues, such as plastics (PE, PP, PET, PVC, etc.), cellulose-containing substances and biomaterials, comprising at least one feed system (100) for the feedstock (7), a reaction unit (10), at least one single or multi-part separation and separation unit (3) and at least one sediment treatment stage (200) for solids and / or sediments, wherein the reaction unit (10) comprises at least one reactor (11) for the treatment of a mixture phase consisting of a liquid carrier phase (carrier oil) and the solid feedstock (7), wherein the reactor (11) in normal operation has a gas- or vapor-filled headspace (11.1) and a product space (11.2) filled with the mixture phase.2) further comprising a reactor inlet (12) for the feedstock (7), a top outlet (13) for a gas or vapor phase, an outlet (14) connected to the sediment treatment stage (200) and at least one motor-driven stirring unit (15) for homogenizing and circulating the reactor contents, which projects into the product space (11.2) with at least one stirring element (16), wherein . the reactor (11) further comprises at least one motor-driven rotary cutting unit (18) for the impact and / or cutting comminution of the starting material (7) and the reactor (11) further comprises at least one heating device (22) or a heating device (22) is directly adjacent to it, characterized in that the reactor inlet (12) is inclined upwards relative to the horizontal (29.2) and the horizontal (29.2) is formed as a theoretical center line running parallel and midway between an upper plane (e1) comprising the height (h1) of the highest point of the upper edge of the reactor inlet (12) and a lower plane (e2) comprising the height (h2) of the lowest point of the lower edge of the reactor inlet (12), wherein the housing of the inlet screw conveyor is directly connected to and / or projects into the reactor inlet (12) or a flange of the reactor (11), wherein the cutting unit (18) is arranged on a theoretical cutting plane (31) which results as a theoretical mean plane of space during the rotational movement of the cutting unit (18), and which is located at a height (h3) that is less than the height (h1) of the upper edge of the reactor inlet (12), and wherein the heating device (22) is at least a microwave heater (22.1) having a power of 80 to 200 kW or more, and which is separated from the product space (11.2) of the reactor (11) or from a circulating line (58) carrying the mixing phase by at least one disk, window and / or pipe made of glass or quartz glass.

Description

[0001] The invention relates to a plant for the catalytic production of diesel oil from residual materials, such as plastics (PE, PP, PET, PVC, etc.), cellulose-containing substances and biomaterials according to the preamble of claim 1. Furthermore, the invention relates to a corresponding method according to the preamble of claim 16.

[0002] From WO 2005 / 071043 A1, a plant is known in which hydrocarbon-containing residues or deposits are heated, cracked, and fractionated in a multi-stage process, thereby producing, among other things, diesel fuel. Furthermore, such a plant is also known from DE103 56 245 B4, in which the main heat input is via the flow energy of the pumps, which are slowed by a counter-rotating agitator as well as by its friction and internal friction. However, it has been found that these plants are still very prone to malfunctions.

[0003] From DE 103 16 696 A1, a precursor for the catalytic oiling of hydrocarbon-containing residues in a liquid circuit is known, wherein ion-exchangeable catalysts, such as calcium aluminum silicate or sodium aluminum silicate, are used as catalysts, which are used in a heated oil bath circuit and cleaned at the heat transfer points, wherein the heating of the oil bath circuit with the suspended catalysts is furthermore carried out by electric heating elements that are arranged concentrically around the reactor tubes.

[0004] The object of the invention is therefore to provide a system and a method that are easier to operate and exhibit less susceptibility to malfunctions.

[0005] This problem is solved by a system according to claim 1, characterized in that the central reactor, which receives the starting material in a carrier oil and in which the catalytic reaction takes place, has at least one motor-driven rotary cutting unit by means of which the starting material is comminuted at least intermittently by impact and / or cutting. A corresponding method is described according to claim 16.

[0006] For the purposes of this text, the starting material shall be understood to be all hydrocarbon-containing raw materials and residues, in particular residual and waste materials from the group of plastics (PE, PP, PET, PVC, etc.), cellulose-containing materials, and biomaterials such as wood, sawdust or wood shavings, paper, cardboard, plant parts, and the like. Furthermore, granular particle size shall be understood to mean free-flowing particles whose maximum spatial dimension has an average dimension of less than or equal to 20 mm, preferably less than or equal to 10 mm. Ideally, these are in the form of shavings, flakes, or similar flat particles.

[0007] In this context, "diesel" or "diesel oil" refers to a kerosene mixture, specifically the middle distillate fractions from known fractionation processes of petroleum. The carrier oil, on the other hand, is a low-boiling heavy oil or heavy oil mixture. Such carrier oils are typically thermal oils that do not decompose at high operating temperatures, such as the range of 280°C to 320°C in this case. Furthermore, so-called secondary refined oils can be used. These are oils that do not undergo chemical reactions, outgassing, or foaming.

[0008] This plant for the catalytic production of diesel oil from the aforementioned feedstock comprises a feed system for the feedstock, a reaction unit, at least one single- or multi-part separation and separation unit, and at least one sediment treatment stage for solids and / or sediments, including ash, tar, and the like. The reaction unit typically includes only one central reactor for treating a mixture of a liquid carrier phase (carrier oil) and the solid feedstock. This reactor is often called a melting reactor because the solids are catalytically converted into diesel oil within it. Ideally, the reactor has only one reactor chamber, but in normal operation, it has a gas- or vapor-filled headspace and a product chamber filled with the mixture. Furthermore, it includes at least...The reactor includes an inlet for the feedstock, at least one outlet for a gas or vapor phase to which a separation column can be directly connected or attached, an outlet connected to the sediment treatment stage, and at least one motor-driven agitator for homogenizing and circulating the reactor contents, which extends into the product chamber with at least one agitator. As described, at least one motor-driven rotary cutting unit is also provided for the impact and / or cutting comminution of the feedstock, which has at least one cutting edge or section.

[0009] In one embodiment of the cutting unit, it is mounted on and driven by the same drive shaft as the at least one agitator, whereby alternatively or additionally the at least one agitator can also be designed as a cutting edge or with a cutting section. Another alternative is that the cutting unit projects into the product chamber and has its own drive shaft and its own drive, independent of the drive of the agitator.

[0010] One improvement is that at least one agitator is arranged in a vertical position between two cutting units, so that these can cut and / or divide directly above and below the agitator in the directed flow.

[0011] The drive must be designed to enable continuous, complete mixing and multiple revolutions per minute, requiring a stirring unit speed of at least 400 to 500 rpm. A rotational speed of 440 to 470 rpm is advantageous. It is beneficial if the peripheral speed of the stirring unit is in the range of 10 to 20 m / s, and ideally, a peripheral speed of 13 to 18 m / s should be achievable and adjustable during operation. Similarly, the drive for the cutting unit should operate at a speed of at least 400 to 500 rpm, with a speed of over 440 to 470 rpm being advantageously maintained during operation.

[0012] A further improvement lies in the fact that the agitator, in particular its drive shaft, is eccentrically arranged within the reactor, resulting in a particularly advantageous three-dimensional flow in the reactor's product chamber. An axial eccentricity E of the agitator axis relative to the reactor's central axis, in the range of 0.15 to 0.25, has proven advantageous.

[0013] The single- or multi-part separation and separation unit downstream of the reactor comprises at least one condenser and / or a separation column for separating the diesel oil. Surprisingly, it has turned out that it is sufficient to provide a simple separation column after the reactor – possibly directly on it – followed by one or two condensers for separating the product oil.

[0014] As indicated, the separation column and the reactor then form a single unit and are attached directly to the headspace or connected to it via a flange. The reactor headspace extends directly into the lowest bottom or inlet area of ​​the column, forming a single chamber.

[0015] Furthermore, a heating device for the mixing phase is provided, which in an improved version is located externally on the reactor wall and acts on the fluid through the vessel wall. Alternatively, such a heating device can be integrated within the reactor. These heating devices are designed and dimensioned to heat the filled mixing phase to over 200 °C, ideally to a temperature between 280 °C and 320 °C.

[0016] According to the invention, a microwave heating device is provided as the heating element, which has proven to be particularly advantageous. This device has a very high efficiency, and unlike conventional heating surfaces, thermally induced adhesion due to local overheating does not occur on the exchange surfaces or the emitting surfaces of the microwave heater. Ideally, at least one such microwave heating device is arranged in the liquid-covered space of the reactor interior. The power output of the microwave generator should be in the range of over 70 kW, ideally in the range of 80 kW to 250 kW. If required, the power output can be higher, or more than one microwave generator can be provided.

[0017] The microwave heating system comprises, as known, a magnetron and a waveguide as its main components. This waveguide typically includes, among other things, at least one glass or quartz glass disk adjacent to and separating it from the product chamber, a tuner for minimizing reflected microwaves, a circulator, a water load, and suitable detectors and directional couplers. In an improved embodiment, the product chamber is bordered not only by a glass or quartz glass disk, but also by a safety airlock with closures on both sides by glass or quartz glass disks, the interior of which can be filled with an inert gas or through which an inert gas can flow. "On both sides" refers to the direction of the main extension of the waveguide in which the microwaves are guided.The advantage is that the interior can be evacuated and, in the event of damage to the pane adjacent to the product chamber, no oxygen enters the reactor and the other components of the microwave heater remain protected.

[0018] An alternative, inventive design consists in the reactor contents not being heated directly by microwave heating through the aforementioned disc in the reactor wall or a mounting nozzle, but rather the at least one microwave heater acting on a side stream of the mixing phase through a glass or quartz glass tube. This side stream in a circulation line is advantageously driven by a suitable conveying device, such as a twin-screw pump.

[0019] For sealing the safety discs of the safety airlock in the hollow channel, paper gaskets or gaskets made of a copper material (soft copper) are advantageously used, thus creating a gas-tight separation. Surprisingly, it has been found that this gas-tight section from the central reactor functions as a very advantageous cooling section.

[0020] In an alternative design, the microwave heating element is located in the reactor's lid and / or headspace. The advantage of this is that placing the microwave heater in the reactor's headspace reduces thermal and mechanical stresses. Furthermore, this design provides good accessibility for maintenance.

[0021] A further improved version involves a recirculation inlet at the reactor, connected to the sediment treatment stage, through which partial flows or quantities extracted via an outlet can be returned to the reactor. These recirculated partial flows or quantities are typically liquid and depleted of solids such as lime, catalyst, ash, or tar.

[0022] The reactor inlet and / or the return inlet are shaped such that a housing of an infeed screw conveyor is held and sealed against them. Known flange or coupling elements can be used for this purpose. It is particularly advantageous if no separate pipe section is required between the reactor inlet and the outlet end of the infeed screw conveyor.

[0023] One improvement is that the housing of the inlet screw conveyor ends directly at the reactor with the outlet end, or forms the reactor flange.

[0024] Process and auxiliary materials, such as carrier oil, lime, or catalyst, can be introduced into one of the other feed or return streams. Advantageously, however, a separate feed unit for process and auxiliary materials is provided, which is connected to the reactor via a pipeline and has its own access port in the reactor.

[0025] Not described in detail, because it is standard practice for the expert, are necessary cable connections, connecting flanges, structural elements and the like, as well as the known and usual control and regulation units.

[0026] By using this plant and in particular the reactor, a process for the continuous production of diesel oil from the aforementioned starting material is possible, which is introduced as a granular solid phase into a liquid phase of the aforementioned carrier oil and catalytically transformed.

[0027] The temperature in the mixing phase is between 200 and 400 °C, ideally between 280 °C and 350 °C. The mixing phase also contains a proportion of lime of 1.5 wt.% to 10 wt.%, where "lime" is used here as a collective term for substances or mixtures containing calcium or calcium carbonate. Furthermore, the mixing phase contains a catalyst in a proportion of 1 wt.% to 15 wt.%.

[0028] The gaseous or vaporous phase is continuously removed, ideally by means of at least one vacuum pump continuously extracted from the reactor headspace. Downstream of the reactor, the diesel oil is separated from the more volatile gaseous or vaporous phase in at least one condenser.

[0029] During the mixing phase, the granular feedstock is mechanically cut and / or comminuted by means of at least one cutting edge or section. For optimal mixing within the reactor and to prevent any sedimentation, the peripheral speed of the agitator is between 8 and 20 m / s, although it has been found that an ideal speed of 13 to 17 m / s is recommended.

[0030] The catalyst is advantageously a bentonite or zeolite, in particular an aluminum silicate, in powder form. The pressure to be set in the reactor headspace is less than or equal to 1 bar, ideally in the range of 25 to 60 mbar.

[0031] Not described in detail, because it is standard practice for the expert, are necessary cable connections, connecting flanges, structural elements and the like, as well as the known and usual control and regulation units.

[0032] The invention is explained in more detail below by way of example, showing Fig. 1. A block diagram showing the process flow and the most important process steps, Fig. 2 the facility after Fig. 1 with individual steps to the product processing stage, Fig. 3 a first embodiment of the central reactor, Fig. 4 a second embodiment of the central reactor, Fig. 5 another embodiment of the central reactor, Fig. 6 the construction of the microwave heating system of the central reactor and Fig. 7 an alternative embodiment to Fig. 6.

[0033] In the Fig. Figure 1 schematically depicts the entire plant 1 for the catalytic production of diesel oil 9 from feedstock 7 as a block diagram. The feedstock 7 is supplied to the reaction unit 10 via the inlet system 100. The reaction unit 10 has at least one reactor, but can also include two or more reactors connected in parallel (not shown). The feedstock 7 is fed into the reactor 11 via the reactor inlet 12, as shown.

[0034] The process and auxiliary materials 8, such as carrier oil, lime, and catalyst, are also introduced via the inlet system 100. Alternatively, but not shown, this can be done via a separate feed unit connected to reactor 11 by a pipeline, for which a separate access port is provided in reactor 11. Furthermore, a product preparation stage 300 for the diesel oil 9 is connected to or attached to the headspace 11.1 of reactor 11 via the head outlet 13. In product preparation stage 300, the diesel oil component is separated from the more volatile aqueous phase in the gas and vapor phases. The diesel oil 9 is stored in storage tank 24.

[0035] Near the bottom, with a connection to product chamber 11.2, reactor 11 is connected via bottom outlet 14 and outlet line 14.1 to a sediment treatment stage 200, from which return line 23.1 leads to return inlet 23, allowing a liquid phase to be returned to reactor 11. Furthermore, system 1 includes an optional coupling and purification unit 400, which can be used, for example, to desulfurize diesel oil 9 and / or to further process and package the solids and sedimentation. For this purpose, product treatment stage 300 and / or sediment treatment stage 200 are appropriately connected to each other via suitable conveying devices and / or lines.

[0036] In Fig. For the sake of clarity, the usual assemblies for control, regulation, conveyance, displays, etc. are not shown in Figure 1 and the figures below.

[0037] As further in Fig. As can be seen in Figure 1, reactor 11 has a stirring unit 15, with a drive 19, a drive shaft 17, a stirring element 16 and a cutting unit 18. In this and the following embodiments, the stirring element 16 is designed as a 2- to 4-bladed propeller.

[0038] The Fig. 2 shows Annex 1 according to Fig. 1 in an embodiment in which the product processing stage 300 for the gas and / or vapor phase leaving the headspace of the reactor 11 via the head outlet 13 comprises a separation and separation unit 3, which includes a separation column 4 and two condensers 5.1, 5.2 connected in series via the steam lines 26.1 and 26.2. These condensers 5.1, 5.2 are operated at a temperature just above the boiling point of water at > 100°C, ideally in a temperature range of 101°C to 105°C. This process allows the volatile vapor phase, which essentially contains the remaining water vapor, to leave the product processing stage 300 via the steam line 26.3 towards the chimney 25. The condensed diesel oil 9 leaves the respective condensers 5.1 and 5.2 via product lines 27.1 and 27.2 and is fed to the storage tank 24 via the collecting product line 27. Starting from one of the product lines 27, 27.1, 27.2 is fed via the return line 28 diesel oil 9 into the separation column 4 at the top to ensure a safe separation process.

[0039] The separator column 4 is filled with a bed 4.1 of inert molded parts, generally metallic components arranged on one or more screen trays. In this case, less than 15% of the total flow of diesel oil is returned to the separator column 4. The separator column 4 does not primarily serve as a distillation column, but rather its purpose is to reliably retain entrained foreign or starting materials, rising foam, and heavy oil droplets in reactor 11.

[0040] Furthermore, the heating device 22 at reactor 11 in the area of ​​product space 11.2 is shown schematically, whereby, as explained above, usual fittings, valves, conveying means, etc. are not shown.

[0041] In the Fig. Figure 3 shows reactor 11 in more detail. The drive shaft 17 of the agitator 15 is arranged parallel and eccentrically to the central axis MA of reactor 11 at a distance E1 and is held on the upper dished head 30.1 by the mounting flange 19.1. The cutting unit 18 has a diameter d1 that is slightly larger than the diameters d2 of the two agitators 16.1 and 16.2, which are mounted above and below the cutting unit 18 on the same drive shaft 17 and driven by it. The distance between the upper edge or flange of the lower dished head 30.2 and the lower edge or flange of the upper dished head 30.1 is the height H1. The height H2 is also measured to the lower edge or flange of the upper dished head 30.1, but has the lowest extent of the lower dished head 30.2 as its lower reference point. The flange of the reactor inlet 12 is angled at α of 30° relative to the horizontal 29.2 inclined upwards, with the horizontal 29.2 passing through the opening at the reactor inlet 12 in the center of the flow area. The horizontal 29.2 thus forms a theoretical center line that runs parallel and centrally between an upper plane e1, which at height h1 encompasses the highest point of the upper edge of the reactor inlet 12, and a lower plane e2, which at height h2 encompasses the lowest point of the lower edge of the reactor inlet 12.

[0042] In the present embodiment, the reactor inlet 12 and the return inlet 23 are shaped such that a pipe or conveying unit can be directly flanged to them, in particular that the housing of an inlet screw conveyor is held and sealed against them (not shown). Known flange or coupling elements can be used for this purpose. It is particularly advantageous if there is no longer a separate pipe section between the reactor inlet and the outlet end of the inlet screw conveyor, and these transition directly into one another. As in the Fig. As can be seen in Figure 3, the return inlet 23 is also inclined by an angle β to the horizontal, which should be in the range of 5° to 35°.

[0043] It has generally been found to be very advantageous if the space spanned by the cutting unit 18 during rotation lies below or encompasses the horizontal 29.2 and ideally lies below the plane e2. In other words, ideally, a theoretical cutting plane 31, as a theoretical mean plane of space resulting from the rotational movement of the cutting unit 18, lies at a height h3 that is less than the height h1 and, in particular, is also less than or equal to the height h2.

[0044] Surprisingly, it was found that a further improvement is achieved when the theoretical cutting plane 31 lies in the space between the horizontal 29.2 and the plane e2. This means that the supplied feedstock is immediately cut and impacted upon entering the reactor 11, resulting in optimal distribution and comminution.

[0045] In the case of a very pronounced, strongly curved lower dished end 30.2, the analogous consideration takes place starting from the lowest point of the dished end.

[0046] The motor power of the drive 19 is in the range of 9 to 15 kW, with a speed of 1,300 to 2,000 rpm. Depending on the gearbox, a drive speed of 400 to 500 rpm is achieved at the agitator 16 in the present embodiment.

[0047] As in the Fig. As can still be seen in Figure 3, the separation column 4 is attached to the top outlet 13 via a connecting flange directly to the upper dished end 30.1 of the reactor 11. The heating device is, in the design according to... Fig. 3. A microwave heater 22.1, with a power output of 100 kW, whose microwaves 22.2, indicated as cubic waves, act directly into the mixing phase. For this purpose, the microwave heater 22.1 is located inside reactor 11.

[0048] An alternative location for the microwave heater 22.1, not shown, is in the headspace 11.1 of reactor 11, because this reduces the thermo-mechanical influences and provides better accessibility in case of maintenance.

[0049] In the version according to the Fig. 4 The stirring unit 15 shown on the left essentially corresponds to the one from Fig. 3, wherein a stirrer 16.1 is provided on one drive shaft 17 and above the cutting unit 18. Furthermore, a second stirrer 15.1 with its own drive 21 and associated drive shaft 20 is provided, on which two further stirrers 16.3, 16.4 are arranged. The advantage is that the upward flow is supported and the drive 19 of the stirrer 15 can be designed to be smaller. Another advantage is that even if one stirrer 15, 15.1 fails, the circulation in the reactor 11 can be maintained, possibly with a reduced or shut-off feed of feed material. The second stirrer 15.1 is also arranged eccentrically by a distance E2, parallel to the central axis MA. Ideally, the two drive shafts and the central axis MA lie in a vertical plane. The main flow direction is indicated by arrows.

[0050] The embodiments and arrangements according to the Fig. 3 and Fig. The four components can be combined depending on the reactor dimensions, in particular the number of agitators and / or cutting edges or cutting sections. For example, a cutting edge or cutting section 18.1 can also be provided on the second or a further agitator (not shown).

[0051] In addition to the previous embodiments and combinable with them, the following is available in the Fig. Figure 5 shows a reactor 11 in which ultrasonic emitters 33.1, 33.2, and 33.3 are provided in the interior. The ultrasonic emitters 33.1 and 33.2 are arranged as rod-shaped emitters at two different heights. The embodiment of a flat ultrasonic emitter is sketched with reference numeral 33.3, the number and power of which depend on the dimensions of the reactor 11. These emitters are preferably attached to the reactor wall or through it via a flange at a certain height in the product chamber 11.2. They are connected to a corresponding control and power supply unit 32 via data and / or power lines 34. The use of ultrasonic emitters improves the homogenization of solid particles in the mixing phase. Surprisingly, it has been shown that even a single flat ultrasonic emitter 33.3 leads to optimal homogenization of solid particles in the mixing phase.

[0052] However, it can be advantageous to provide several ultrasonic emitters at different height levels, so that when the level of the mixing phase drops, only the uncovered ultrasonic emitters can be switched off, while the ultrasonic emitters covered with fluid (mixing phase) continue to operate.

[0053] In the Fig. 6 and Fig. Figure 7 shows the installation situations and construction of the microwave heater 22.1 in detail and is otherwise analogous to the design according to Fig. 3 trained. This shows the Fig. 6 one of possibly several microwave heaters 22.1, which are arranged directly on the outer wall of the central reactor 11. The microwave heater 22.1 has a magnetron 37, a waveguide 38 and a safety airlock 36, which abuts the reactor 11 at one end and at the safety disc 36.2 arranged there.

[0054] Standard flange and connecting elements are provided, but not detailed. An inert gas, e.g., nitrogen, can be introduced into the interior 36.1 of the safety airlock 36 via the inlet 36.3. A further safety disc 36.4 is arranged at the second end of the safety airlock 36; both safety discs 36.2 and 36.4 are made of glass or quartz glass. The magnetron 37 generates the microwaves, which are indicated by a strong arrow pointing towards reactor 11. Other known elements of the microwave heating system are mentioned only, without detailed illustration, such as a tuner for minimizing reflected microwaves (indicated by a narrow arrow), a circulator, a water load, as well as suitable detectors and a directional coupler.

[0055] In this advantageous embodiment, the product chamber 11.2 is bordered not only by a single glass or quartz glass pane 36.2, but by a safety airlock 36, whereby in a simplified design only a single safety pane 36.2 can be provided between the product chamber 11.2 of the reactor 11 and the microwave heater 22.1.

[0056] Alternatively to Fig. 6 shows Fig. 7 An alternative design is described in which the mixture phase filled into product chamber 11.2 is not heated directly. Instead, a line 58 is provided, which circulates in and out of the reactor and in which a conveying medium 59, such as a double-screw pump, operates. Furthermore, a glass or quartz glass tube 39 is provided as a section of the line 58, through which the microwaves from two microwave heaters 22.1a, 22.1b act on the flowing mixture phase. To avoid excessive back-emission of the microwaves into the microwave heaters, it can be advantageous to provide several glass or quartz glass tubes 39 on different sections of the line 58, each with its own individual microwave heater 22.1a, 22.1b.

[0057] In the variant shown, the pipeline has 58 microwave heaters 22.1a, 22.1b of two different designs. The microwave heater 22.1a, located closer to reactor 11, is constructed as shown in Fig. 6 described, wherein the microwave heater 22.1b arranged downstream for this purpose does not include a safety lock and only one or more windows made of glass or quartz glass are provided through which the microwaves are directed into the interior of the tube.

[0058] As already mentioned, it is advantageous to provide one or more ultrasound emitters.

[0059] It has proven advantageous, for example, if a copper-based seal is provided on at least one side, ideally on both sides, as the sealing material for the first safety disc 36.2, which borders the inner tube space and / or product space 11.2 carrying the mixing phase. On the second side of the safety channel 36, the side facing away from the first, a fluororubber seal is provided for the inner side of the safety disc, and a cooling flange made of an aluminum alloy is provided on the outer side facing the magnetron.

[0060] The components not shown in part can be provided individually or collectively as described above, in particular the microwave heater 22.1 and / or the ultrasonic emitters 33. Reference symbol list 1 Annex 2. Supply of auxiliary materials 3 Separation and separation unit 4 Separation column 4.1 Filling 5 capacitors 5.1 Capacitor 5.2 Capacitor 6 Inert gas 7 Starting material 8 Auxiliary and process media 8.1 Tank 8.2 Funding 9 Diesel oil / line 10 reactor units 11 Reactor 11.1 Headspace 11.2 Product space 12 Reactor inlet 12.1 Admission Management 13 Head outlet 14 floor outlet 14.1 Outlet pipe 15 Mixing unit 16 stirring elements 16.1 Stirring element first 16.2 Stirring body second 17 Drive shaft 17.1 Drive 18 cutting unit 18.1 Cutting edge or cutting section 19 Drive 19.1 Mounting flange 20 Drive shaft 21 Drive 22 Heating system 22.1 Microwave heater 22.2 Microwave 23 Return entrance 23.1 Return line 24 storage tank 25 fireplace 26 Steam line 26.1, 26.2, 26.3 27 Product Management 27.1, 27.2 28 Return line 29 Horizontal 29.1 Middle of H1 29.2 Horizontal line in the center of the flow area 30 dished heads 30.1 upper dished head 30.2 lower dished head 31 Cutting plane 32 Control and supply unit 33 Ultrasound emitters 32.1, 32.2, 32.3 34 Data and / or power line 35 ultrasound waves 36 Security gate 36.1 Interior 36.2 Safety glass 36.3 Admission 36.4 Safety glass 37 Magnetron 38 waveguides 39 Glass or quartz glass tube 58 Management 59 funding opportunities 100 Induction system 200 Sediment processing stage (sediment) (new) 300 Product processing stage (product) (new) 400 coupling and cleaning unit e1 plane, horizontal e2 plane, horizontal E1 Eccentricity E2 eccentricity H1 Height of reactor interior without dished end H2 height reactor interior with lower dished end h1 Height of the upper edge of the inlet h2 Height of the lower edge of the inlet h3 Height of the cutting unit α, β angles MA Central Axis

Claims

[1] Plant (1) for the catalytic production of diesel oil (9) from a feedstock (7) from the group of residues, such as plastics (PE, PP, PET, PVC, etc.), cellulose-containing substances and biomaterials, comprising at least one feed system (100) for the feedstock (7), a reaction unit (10), at least one single or multi-part separation and separation unit (3) and at least one sediment treatment stage (200) for solids and / or sediments, wherein the reaction unit (10) comprises at least one reactor (11) for the treatment of a mixture phase consisting of a liquid carrier phase (carrier oil) and the solid feedstock (7), wherein the reactor (11) in normal operation has a gas- or vapor-filled headspace (11.1) and a product space (11.2) filled with the mixture phase.2) further comprising a reactor inlet (12) for the feedstock (7), a top outlet (13) for a gas or vapor phase, an outlet (14) connected to the sediment treatment stage (200) and at least one motor-driven stirring unit (15) for homogenizing and circulating the reactor contents, which projects into the product space (11.2) with at least one stirring element (16), wherein. the reactor (11) further comprises at least one motor-driven rotary cutting unit (18) for the impact and / or cutting comminution of the starting material (7) and the reactor (11) further comprises at least one heating device (22) or a heating device (22) is directly adjacent to it, characterized by , that the reactor inlet (12) is inclined upwards relative to the horizontal (29.2) and the horizontal (29.2) is formed as a theoretical center line running parallel and midway between an upper plane (e1) comprising the height (h1) of the highest point of the upper edge of the reactor inlet (12) and a lower plane (e2) comprising the height (h2) of the lowest point of the lower edge of the reactor inlet (12), wherein the housing of the inlet screw conveyor is directly connected to and / or projects into the reactor inlet (12) or a flange of the reactor (11), wherein the cutting unit (18) is arranged on a theoretical cutting plane (31) which results as a theoretical mean plane of space during the rotational movement of the cutting unit (18), and which is located at a height (h3) that is less than the height (h1) of the upper edge of the reactor inlet (12), and wherein the heating device (22) is at least a microwave heater (22.1) having a power of 80 to 200 kW or more, and which is separated from the product space (11.2) of the reactor (11) or from a circulating line (58) carrying the mixing phase by at least one disk, window and / or pipe made of glass or quartz glass. [2] Plant (1) according to claim 1, characterized by, that the at least one cutting unit (18) has at least one cutting edge or cutting section (18.1) and is attached to and driven by the same drive shaft (17) as the at least one agitator (16) and / or that the at least one agitator (16) is designed as a cutting edge or with a cutting section (18.1). [3] Plant (1) according to claim 1, characterized by , that the cutting unit (18) has a drive shaft (20) and its own drive (21) which is independent of the drive (19) of the stirring unit (15). [4] Plant (1) according to claim 1, characterized by , that at least one cutting unit (18) is arranged in a vertical position between two agitators (16.1, 16.2). [5] Annex (1) according to any of the preceding claims, characterized by, that the drive (19) enables the speed of the agitator (15) to be at least 400 to 500 rpm and / or a peripheral speed of the agitator (15) of 10 to 20 m / s is achievable. [6] Annex (1) according to any of the preceding claims, characterized by , that the drive (21) of the cutting unit (18) enables a speed of at least 400 to 500 rpm. [7] Annex (1) according to any of the preceding claims, characterized by , that the agitator (15) and / or its drive shaft (17) is arranged eccentrically in the reactor (9). [8] Annex (1) according to any of the preceding claims, characterized by , that the single or multi-part separation and separation unit (3) comprises at least one condenser (5) and / or a separation column (4) for separating the diesel oil (9). [9] Plant (1) according to claim 8, characterized by, that downstream of the reactor (11) the separation column (4) and subsequently the at least one condenser (5) are arranged . [10] Annex (1) according to claim 8 or 9, characterized by , that the separation column (4) forms a structural unit with the reactor (11) and is directly attached to or connected with the headspace (11.1). [11] Annex (1) according to any of the preceding claims, characterized by , that the at least one heating device (22) is designed to achieve a heating of the filled mixing phase to between 280 °C and 350 °C. [12] Annex (1) according to any of the preceding claims, characterized by , that the at least one microwave heater (22.1) includes a safety lock (36) as a waveguide section which has an evacuatable interior (36.1). [13] Annex (1) according to any of the preceding claims, characterized by, that a return inlet (23) is provided at the reactor (11) which is connected to the sediment preparation stage (200) and through which partial streams or partial quantities that were taken out via the outlet (14) can be returned to the reactor (11). [14] Annex (1) according to any of the preceding claims, characterized by , that the reactor inlet (12) and the return inlet (23) are shaped in such a way that a housing of an inlet screw conveyor is held and sealed against them. [15] Annex (1) according to any of the preceding claims, characterized by , that a supply unit (2) for process and auxiliary materials (8) is provided, which is connected to the reactor (11) by a pipeline. [16] Process for the continuous production of diesel oil from a starting material (7) from the group of residues, such as plastics (PE, PP, PET, PVC, etc.), cellulose-containing materials (sawdust, shredded material) and biomaterials, which is introduced as a granular solid phase into a liquid phase of a carrier oil and catalytically transformed, characterized by , that a system (1) is provided according to any one of the preceding claims 1 to 15, and wherein - the temperature during the mixing phase between 280°C and 350°C and - the mixture phase continues to have a proportion of lime of 1.5 wt.% to 10 wt.% and a proportion of catalyst of 1 wt.% to 15 wt.%, and wherein - the gaseous or vaporous phase is continuously extracted from the headspace (11.1) by means of at least one vacuum pump and downstream of the reactor (11) the diesel oil (9) is separated from the volatile gaseous or vaporous phase in at least one condenser (5). [17] Method according to claim 16, characterized by , that the starting material (7) contained in the mixture phase is mechanically comminuted by means of the at least one cutting edge or cutting section (18.1) in the reactor (11). [18] Method according to one of claims 16 or 17, characterized by that the catalyst is a bentonite, zeolite or aluminum silicate. [19] Method according to any one of claims 16 to 18, characterized by , that the peripheral speed of the stirring unit (15) is between 8 and 20 m / s. [20] Method according to any one of claims 16 to 19, characterized by , that the pressure in the headspace (11.1) of the reactor (11) is less than or equal to 1 bar.

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