DE102019001702A1 - Plant and process for the catalytic production of diesel oils from organic materials - Google Patents

Abstract

Plant and process for the catalytic production of diesel oil from a starting material from the group of residues, such as plastics (PE, PP, PET, PVC, etc.), cellulose-containing substances and biomaterials, comprising at least one feed system for the solid starting material, a reaction unit, at least a one-part or multi-part separation and separation unit and at least one sediment treatment stage for solids and / or sediments, the reaction unit having a reactor for treating a mixed phase of a liquid carrier phase and a solid starting material, the reactor having an inlet for the starting material, a head outlet for the gas or vapor phase and an outlet which is connected to the discharge system, as well as at least one motor-driven agitator unit for homogenizing and circulating the reactor contents, the reactor also having a motor-driven rotary cutter for beating and / or cutting Ze reduction of the raw material.

Description

The invention relates to a system for the catalytic production of diesel oil from residues 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 Preamble of claim 18.

From the WO 2005/071043 A1 a system is known in which residues or residues containing hydrocarbons are heated, cracked and fractionated in a multi-stage process, whereby, among other things, diesel oil is obtained. Furthermore, from the DE103 56 245 B4 Such a system is also known, the main heat input taking place via the flow energy or the friction and internal friction of the pumps, which are braked by a counter-rotating agitator. However, it has been found that these systems are still very susceptible to failure.

The object of the invention is therefore to provide a system and a method that can be operated more easily and is less susceptible to failure.

This object is achieved by a system according to claim 1, which is 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 cutter, by means of which at least temporarily a beating and / or cutting comminution of the starting material takes place. A corresponding method is achieved according to claim 18.

All raw and residual materials containing hydrocarbons should be considered as the starting material, 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 chips, paper, Cardboard, plant parts and the like. Furthermore, a granular particle size is to be understood as meaning free-flowing particles which, in their largest spatial extent, have on average less than or equal to 20 mm, advantageously less than or equal to 10 mm. Ideally, these are designed as chips, flakes or comparable flat particles.

In the present case, diesel or diesel oil is to be understood as meaning a kerosene mixture, the so-called middle distillate fractions in the case of known fractionations of petroleum. The carrier oil, on the other hand, is a lower-boiling heavy oil or heavy oil mixture. Such carrier oils are generally thermal oils which do not decompose at high operating temperatures, as in the present case, for example, in the range from 280 ° C to 320 ° C. So-called secondary refiners can also be used. These are oils that do not lead to chemical reactions, outgassing or foaming.

This plant for the catalytic production of diesel oil from the aforementioned starting material comprises a feed system for the starting material, a reaction unit, at least one one-part or multi-part separation and separation unit and at least one sediment processing stage for solids and / or sediments, among others. such as ashes, tar matter, and the like. The reaction unit generally comprises only one central reactor for treating a mixed phase of a liquid carrier phase (carrier oil) and the solid starting material, the reactor often also being called a melt reactor, because in this the solids are catalytically converted into diesel oil. The reactor ideally has only one reactor interior, but in normal operation it has a gas or steam-filled head space and a product space filled with the mixed phase. Furthermore, it comprises at least one inlet for the starting material, at least one top outlet for a gas or vapor phase, to which a separation column can directly adjoin or be attached. There is also an outlet that is connected to the sediment processing stage, as well as at least one motor-driven agitator for homogenizing and circulating the reactor contents, which protrudes into the product space with at least one agitator.

The sediment processing stage for discharging and separating solid ingredients from the product space comprises a conveying unit, a sedimentation tank, a discharge element arranged vertically below the sedimentation tank or close to the bottom in the sedimentation tank. This diverting element is designed as a scratching or grinding conveying means, in particular as a screw conveyor and is used to remove oily solids. Furthermore, the sedimentation vessel is connected to a return inlet of the central reactor via a motor-driven transport element, which is designed as a scraping or scraping conveyor, such as a conveyor screw. In the case of a screw conveyor, this is ideally designed as a pulling screw conveyor so that no residues or contaminants affect the sealing materials mechanically. This has the great advantage over a conventional pump that the entire conveying path is permanently kept mechanically free and no local adhesions and cross-sectional constrictions can occur.

The sedimentation kettle serves as a separator and ideally has a conical or funnel-shaped bottom. The separation in the sedimentation tank can be increased if the inlet line is inclined in relation to the radius in the horizontal plane, so that the liquid can flow in in the circumferential direction and constant liquid vortices are formed and a type of cyclone separation is thereby initiated.

An improvement is that the motor-driven, return transport element in the upper third of the sedimentation vessel is connected to the latter and / or protrudes into it with the inlet end. Furthermore, the return transport element can protrude into the reactor with the end remote from the sedimentation vessel and / or be connected to it in a sealing manner. It is particularly advantageous if this returning transport element has a gradient in the direction of the sedimentation tank to the reactor in the conveying direction, i.e. is inclined to the horizontal. An angle in the range from 10 ° to 45 ° has proven to be advantageous.

In one embodiment, the sedimentation boiler has a motor-driven scraper and scraper element, which improves the discharge of the deposited fractions, such as ash, solids, lime fractions, etc. as heavy oily sludge.

In one system variant, the sedimentation boiler is connected to a coupling and purification unit via this diverting element, which comprises a drying and evaporating unit for these oily solids (oil sludge) and / or a separation unit for the steam and / or gas constituents.

As described, there is also at least one motor-driven, rotationally driven cutting mechanism for the percussive and / or cutting comminution of the starting material, which has at least one cutting edge or a cutting section.

In one embodiment of the cutting mechanism, it is attached to and driven by the same drive shaft as the at least one stirring body, wherein the at least one stirring body can alternatively or additionally be designed as a cutting edge or with a cutting section. Another alternative is that the cutting mechanism protrudes into the product space and has its own drive shaft and its own drive that is independent of the drive of the stirring unit.

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

The drive must be designed in such a way that it enables permanent, complete mixing and multiple circulations per minute, for which purpose it must enable a speed of the agitator of at least 400 to 500 rpm. A revolution of 440 to 470 rpm is advantageously carried out. It is advantageous if the circumferential speed of the agitator is in the range of 10 to 20 m / s, and ideally a circumferential speed of 13 to 18 m / s can be achieved by means of the drive and set during operation of the system. The same applies to the drive of the cutting unit that a speed of at least 400 to 500 rpm should be present, with a speed of over 440 to 470 rpm advantageously being maintained during operation.

Another improvement is that the agitator, in particular its drive shaft, is arranged eccentrically in the reactor, whereby a particularly advantageous three-dimensional flow is established in the product space of the reactor. An axial eccentricity of the stirrer axis to the central axis of the reactor which is in the range from 0.15 to 0.25 has proven to be advantageous.

The one-part or multi-part separating and separating unit connected downstream from the reactor comprises at least one condenser and / or a distillation column for separating the diesel oil. It has surprisingly been found that it is sufficient to provide a simple separation column after the reactor - possibly directly on top of it - in order to subsequently provide one or two condensers for separating the product oil.

As indicated, the separation column then forms a structural unit with the reactor and is attached directly to the head space or directly connected to it via a flange. The head space of the reactor extends directly into the lowest floor or inlet area of the column and forms a single space.

Furthermore, a heating device is provided for the mixed phase which, in an improved variant, is provided as a device resting on the outside of the reactor wall and acting on the fluid through the container wall. Alternatively, such a heating device can be included in the reactor. These heating devices are designed and dimensioned so that a filled mixed phase can be heated to over 200 ° C, ideally to a temperature between 280 ° C and 320 ° C.

A microwave heating device has proven to be particularly preferred as the heating device. This has a very high degree of efficiency and, as with conventional heating surfaces, there is no thermally induced adhesion due to local overheating on the exchange surfaces or the emitting surfaces of the microwave heater. At least one such microwave heating device is ideally arranged in the liquid-filled space of the interior of the reactor. The power of the microwave generator should be in the range of over 70kW, ideally in the range of 80kW to 250kW. If necessary, the power can also be higher or more than one microwave generator can be provided.

The microwave heater comprises a magnetron and a waveguide as main components in a known manner. This waveguide usually includes at least one glass or quartz glass pane adjoining and separating the product space, a tuner to minimize the reflected microwaves, a circulator and a water load, as well as suitable detectors and directional couplers. In an improved embodiment, the product space is not only adjoined by a glass or quartz glass pane, but a safety lock with a double-sided closure by a glass or quartz glass pane, the interior of which can be filled with an inert gas or through which an inert gas can flow. In this context, both sides are to be understood as 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 adjoining the product space, no oxygen can get into the reactor and the other components of the microwave heating remain protected.

An alternative design is that the reactor contents are not heated directly by the aforementioned disk in the reactor wall or a fastening nozzle by means of microwave heating, but rather the at least one microwave heating acts on a side stream of the mixed phase through a glass or quartz glass tube. This side stream in a circulation line is advantageously driven by a suitable conveying means, such as a twin screw pump.

To seal the safety panes of the safety lock in the hollow channel, paper seals or seals made of a copper material (soft copper) are advantageously provided so that a gas-tight separation is produced. It has surprisingly been found that this gas-tight section from the central reactor functions as a very advantageous cooling section.

In an alternative embodiment, the position of the microwave heater is in the cover and / or head space of the reactor, which has the advantage that the thermal and mechanical influences are reduced. Furthermore, there is good accessibility in the event of maintenance.

Furthermore, an improved variant consists in that a recirculation inlet is provided on the reactor, which is connected to the sediment processing stage and via which partial flows or partial quantities that were withdrawn via an outlet can be returned to the reactor. The returned partial flows or partial amounts are usually liquid and enriched in solids, such as lime, catalyst, ash or tar fractions.

The reactor inlet and / or the return inlet are shaped in such a way that a housing of an introducing screw conveyor is held on and sealed off. Known flange or coupling elements can be provided 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 introducing screw conveyor.

An improvement is that the housing of the feed screw ends directly at the reactor with the outlet end or forms the reactor flange.

Process and auxiliary materials, such as a carrier oil to be supplemented, lime, catalyst, can be introduced into one of the other feed or return streams. Advantageously, however, a separate supply unit for process materials and auxiliary materials is provided, which is connected to the reactor in terms of lines, with a separate access port being provided in the reactor for this purpose.

Necessary line connections, connecting flanges, structural elements and the like, as well as the known and customary control and regulation units, are not described in detail because they are customary for the person skilled in the art.

Using this system and in particular the reactor, a process for the continuous production of diesel oil from the aforementioned starting material is thus possible, which is introduced as a granular solid phase into a liquid phase from the aforementioned carrier oil and is catalytically converted.

The temperature in the mixing phase is between 200 and 400 ° C, and is ideally between 280 ° C and 320 ° C. The mixed phase also includes a proportion of lime of 1.5% by weight to 10% by weight (2-5), with lime here as a collective term is to be understood as referring to substances or mixtures of substances containing calcium or calcium carbonate. The mixed phase also comprises a catalyst in a proportion of 1% by weight to 15% by weight (2-10).

The gas or vapor phase is continuously removed, ideally continuously withdrawn from the headspace of the reactor by means of at least one vacuum pump. Downstream of the reactor, the diesel oil is separated from the more volatile gas or vapor phase in at least one condenser.

In this case, in parallel in the mixing phase, the garannular starting material contained is mechanically cut and / or comminuted by means of the at least one cutting edge or the cutting section. For optimal mixing in the interior of the reactor and to avoid any sedimentation, the peripheral speed of the stirring unit is between 8 and 20 m / s, whereby it has been found that this should ideally be between 13 and 17 m / s.

The catalyst is advantageously a bentonite or zeolite, in particular an aluminum silicate, which is in a powdery state. The pressure level in the head space of the reactor is less than or equal to 1 bar and is ideally in the range from 25 to 60 mbar.

• 1 als Blockdiagramm einen Verfahrensablauf und die wichtigsten Verfahrensschritte,
• 2 schematisch den Aufbau der Sedimentaufbereitungsstufe,
• 3 eine Schnittdarstellung durch den Sedimentationskessel auf Höhe des Einlassstutzens,
• 4 eine zweite Variante der Sedimentationsstufe,
• 5 eine dritte Variante der Sedimentationsstufe und
• 6 den Aufbau der Mikrowellenheizeinrichtung des zentralen Reaktors.

The invention is explained in more detail below by way of example, and shows

• 1 a block diagram of a process sequence and the most important process steps,
• 2 schematically the structure of the sediment processing stage,
• 3 a sectional view through the sedimentation tank at the level of the inlet nozzle,
• 4th a second variant of the sedimentation stage,
• 5 a third variant of the sedimentation stage and
• 6th the construction of the microwave heating device of the central reactor.

In the 1 is a schematic of the entire system 1 for the catalytic production of diesel oil 9 from the starting material 7th shown as a block diagram. The starting material 7th is via the delivery system 100 the reaction unit 10 fed, which has at least one reactor, but can also include two or more reactors connected in parallel (not shown). The starting material 7th is placed in the reactor as shown 11 via the reactor inlet 12 fed.

There is also a product preparation stage 300 for the diesel oil 9 wired with or on the headspace 11.1 of the reactor 11 via the head outlet 13 connected. In the product preparation stage 300 the diesel oil fraction is separated from the lower-boiling aqueous phase from the gas and vapor phases. The diesel oil 9 is in the storage tank 24 stored.

Close to the floor with a connection to the product area 11.2 is the reactor 11 via the floor outlet 14th and the outlet pipe 14.1 with a sediment treatment stage 200 connected, from the into the return inlet 23 the return line 23.1 leads so that a liquid phase enters the reactor 11 can be directed back. The plant also includes 1 a coupling and purification unit 400 which is optional and by means of which the diesel oil 9 For example, it can be desulfurized and the solids and sedimentation materials can be further processed and packaged. For this purpose are the product preparation stage 300 and / or the sediment treatment stage 200 connected to one another in a suitable manner via suitable conveying means and / or lines.

In 1 and the following figures, conventional units for control, regulation, promotion, displays, etc. are not shown for the sake of clarity.

As continued in 1 to see the reactor points 11 a stirring unit 15th , with one drive 19th , a drive shaft 17th , a stirring body 16 and a cutting unit 18th on. The stirring body 16 is designed in this and the following exemplary embodiments as a 2- to 4-bladed propeller.

2 shows the sediment preparation stage 200 more in detail, the pipeline via the floor outlet 14th and the return inlet 23 with the reactor 11 connected is. The outlet line 14.1 leads to a sedimentation kettle 60 , in which solids such as lime, ash, tar, etc. are separated from a lighter oil phase by sedimentation. In the outlet line 14.1 , advantageously near the floor outlet 14th , is the grant 61 arranged, which is ideally a pump that is well suited for outgassing mixed and sludge phases with solids, such as a screw pump or a screw pump.

The sedimentation kettle 60 advantageously has a motor-driven scraper stirrer 64 on, which the sunk, high-solids oil sludge continuously to the inlet below the sedimentation vessel 60 arranged sludge screw conveyor 63 pushes. This sludge screw conveyor 63 shows the drive 63.1 on and is ideally designed as a plug screw or twin screw, so that a large proportion of the liquid content in this oil sludge enters the sedimentation vessel 60 is pushed back. At the outlet of the sludge screw conveyor 63 the moist, oily residue is placed in a waste collection container 65 directed.

Like in the 3 The sedimentation kettle is easy to see 60 in the lower boiler section 60.3 conical or funnel-shaped and its inlet nozzle 60.1 that is via the outlet line 14.1 with the floor outlet 14th of the reactor 11 connected is to the radius R60 around the angle δ inclined to the angle δ in the example shown is 45 °. The radius R60 extends in a horizontal plane (sectional plane) from the center to the theoretical intersection of the circumference of the sedimentation kettle 60 with the perpendicular to the free flow surface of the inlet connection 60.1 . Above this is the deposition in the sedimentation tank 60 increased, because the introduced mixed phase containing solids flows in in the circumferential direction and thus a constant fluid vortex is formed, which causes a kind of cyclone separation. Furthermore is the outlet 60.2 at the bottom of the sedimentation kettle 60 shown, the transition to the sludge screw conveyor 62 or their connection flange forms. At the bottom of the sedimentation kettle 60 are the two paddles 64.1 of the scraper 64 to recognize.

In the 2 is also shown that the diesel oil 9 from the product preparation stage 300 over the line 27 into the storage tank 24 and a volatile gas phase to the chimney 25th is directed. The coupling and purification unit is also shown 400 , the line-wise with the aforementioned product preparation stage 300 connected is. In particular, however, the waste collection container 65 already part of the coupling and purification unit 400 by further treating the residues via evaporators, compactors or other separating and convection agents.

As in the 2 , 4th and 5 The return screw conveyor is easy to see 62 inclined downwards in the transport direction. The inlet side 62.1 is with the sedimentation kettle 60 connected and the outlet side 62.2 is analogous to the introductory screw conveyor 42 described, directly to the return inlet 23 of the reactor 11 connected and / or introduced into this. The angle of inclination β the return screw 62 is approx. 10 °. The great advantage is that the line path is completely and constantly mechanically cleared and kept clear by the rotation of the screw. The drive 62.3 the return screw 62 is on an extended drive shaft 62.4 from the interior of the sedimentation kettle 60 led out. The further advantage is that in the event of a breakdown or maintenance the driving core of the return screw 62 to the side of the overhead drive 62.3 can be drawn, largely without the contents of the sedimentation kettle 60 or the reactor 11 must be drained.

As in the 2 and 4th regarding the sludge screw conveyor 63 It is easy to see that the conveyor unit was tilted there for the same reasons. In the example shown, this is inclined by 45 ° to the horizontal. However, the sludge auger will rise 63 in the conveying direction, on the one hand, to reduce the overall height of the system 1 to enable and continue the core of the sludge screw conveyor 63 in the direction of the drive 63.1 to be able to draw without affecting the contents of the container 60 or 65 to have to act.

In an alternative, not shown arrangement of the system 1 , can change the altitude of the container 11 , 60 , 65 be chosen so that the sludge screw conveyor 63 leads down in the transport direction and at the same time the drive 63.1 is on top and thus directly under the sludge screw conveyor 63 would be arranged.

The ones in the 4th The system variant shown corresponds to that in 2 embodiment shown. The extension concerns a safety circuit, which the tank shown 70 as a safety tank. In this tank 70 In the event of a malfunction and / or maintenance, the content of the reactor 11 over the lines 14.1 , 71.1 or the sedimentation kettle 60 over the lines 72 , 71.1 be drained. In the case of special malfunctions, the waste collection container can also be filled directly 65 over the lines 14.1 , 71.1 and 71.3 possible. The usual valves, funds, etc. are not shown.

The tank too 70 is advantageously with a heating device 70.1 and an agitator 70.2 upgraded to get the mixed phase eligible.

To improve the homogenization of the solid particles in the reactor 11 is this in the product room 11.2 with an ultrasonic emitter 33 equipped with a control and supply unit via appropriate lines 32 connected is. The ultrasonic waves work here 35 also beneficial to the return inlet 23 and the one there in the return screw 62 pending mixed phase and prevents sedimentation.

The reactor according to the exemplary embodiment of the plant 1 of the 4th is also with an internal microwave heating 22.1 equipped in Gas compartment 11.1 below the dished bottom 30.1 is appropriate. Alternatively, one or more microwave heaters can be used 22.1 also in the product room 11.2 be arranged (not shown).

The execution of the plant 1 to 5 is comparable to that after 2 and shows an alternative embodiment of the sedimentation kettle 60 holding a heater 60.1 includes and also with a motor-driven scraper stirrer 64 Is provided. The very draining sludge screw conveyor 63 is horizontally aligned in the present case and releases the oil sludge, which is heavily enriched with solids, ashes and tar, via a shut-off device 67 into the waste collection container 65 .

The funding 61 in the area of the floor outlet 14th of the reactor 11 is a screw or screw pump that is particularly suitable for pumping hot, outgassing mixed phases

Furthermore shows the 5 the supply line for auxiliary and process media 8th , such as the heavy or carrier oil, lime or catalyst, as well as a mixing and storage tank 8.1 . Conveyance means, other fittings, etc. that are usual for the person skilled in the art are not shown. With the reference number 22nd the heating device is marked with which the filled mixed phase in the product space 11.2 is heated or kept at temperature. The reactor is used for optimal mixing 11 with an agitator 15th equipped with a common drive shaft 17th drives, on which a first agitator 16.1 above the separator 18th and underneath a second stirring body 16.2 is attached.

In the 6th is the installation situation and structure of the microwave heating 22.1 shown in detail. This can otherwise be provided in a single or multiple manner analogously in all the embodiment variants of the previous figures. The 5 one of possibly several microwave heaters 22.1 which is directly on the outer wall of the central reactor 11 are arranged. The microwave heating 22.1 exhibits a magnetron 37 , a waveguide 38 and a security gate 36 on, the one with a first end and the safety disc arranged there 36.2 to the reactor 11 adjoins.

Usual flange and connecting elements are provided, but not detailed. In the interior 36.1 the security gate 36 can through the inlet 36.3 an inert gas, e.g. nitrogen, into the interior 36.1 be directed. At the second end of the security gate 36 is another safety disc 36.4 arranged, both safety discs 36.2 , 36.4 are made of a glass or quartz glass. The magnetron 37 generates the microwaves as a powerful arrow pointing in the direction of the reactor 11 indicates are indicated. Only mentioned, without detailed representation, are the other known elements of microwave heating, such as a tuner to minimize the reflected microwaves, which are indicated as a narrow arrow, a circulator, a water load, as well as suitable detectors and a directional coupler.

In this advantageous embodiment it is adjacent to the product space 11.2 not just a single sheet of glass or quartz glass 36.2 but a security gate 36 , with a simplified design also only a single safety disc 36.2 between product space 11.2 of the reactor 11 and microwave heating 22.1 can be provided.

In a design not shown for 5 becomes the one in the product room 11.2 mixed phase filled in is not heated immediately. Rather, a line is provided which circulates out of the reactor and back in again and in which a conveying means, such as a double spindle pump, operates. Furthermore, a glass or quartz glass tube is provided as a section of the line, via which the microwaves from two microwave heaters 22.1 act on the flowing mixed phase. To avoid excessive reflection of the microwaves in the microwave heater 22.1 it can be advantageous to provide several glass or quartz glass tubes on different line sections, each with a single microwave heater.

As already mentioned, it is advantageous if one or more ultrasonic emitters are provided.

It has been found to be advantageous if, for example, as a sealing material for the first safety pane 36.2 that to the pipe interior and / or product space leading the mixed phase 11.2 a seal made of a copper material is provided at least on one side, ideally on both sides. On the second side of the safety channel facing away from it 36 A fluororubber is provided to seal the inside of the safety pane and a cooling flange made of an aluminum material is provided on the outside facing the magnetron.

The units, some of which are not shown, can be provided individually or collectively as stated above, in particular the microwave heating 22.1 and / or the ultrasonic emitters 33 concerning.

The above exemplary embodiments are greatly simplified, with the usual elements for process management, maintenance, monitoring and control being to be provided by the person skilled in the art as required. Furthermore, for the sake of clarity, not all elements are shown in all the figures, although combinability is fundamentally given and is expressly suggested.

List of reference symbols

1

investment

4th

Separation column

7th

Raw material

8th

Auxiliary and process media

8.1

tank

8.2

Funding

9

Diesel oil / pipe

10

Reactor unit

11

reactor

11.1

Headroom

11.2

Product room

12

Reactor inlet

12.1

Inlet pipe

13

Head outlet

14th

Floor outlet

14.1

Outlet pipe

15th

Agitator

16

Agitator

16.1

Agitator body first

16.2

Stirring body second

17th

drive shaft

18th

Cutting unit

18.1

Cutting edge or cutting section

19th

drive

22nd

Heating device

22.1

Microwave heating

22.2

microwave

23

Return inlet

23.1

Return line

24

Storage tank

25th

stack

26th

casing

27

Product management

32

Control and supply unit

33

Ultrasonic emitter

34

Data and / or power line

35

Ultrasonic waves

36

Security gate

36.1

inner space

36.2

Safety glass

36.3

inlet

36.4

Safety glass

37

Magnetron

38

Waveguide

39

Glass or quartz glass tube

60

Sedimentation kettle

60.1

Inlet port

60.2

Outlet opening

60.3

Cup section, conical

61

Funding

62

Return screw

62.1

Inlet side

62.2

Outlet side

62.3

drive

62.4

drive shaft

63

Sludge screw conveyor

64

Scraper

64.1

paddle

64.2

drive shaft

65

Residual waste collection container

67

Shut-off device

70

Sedimentation kettle

70.1

Heating device

70.2

Agitator

71

management

71.1

Supply line

71.2

Return line

71.3

Supply line

72

management

100

Delivery system

200

Sediment processing stage

300

Product preparation stage

400

Coupling and purification unit

α, β, γ, δ

angle

MA

Central axis

QUOTES INCLUDED IN THE DESCRIPTION

This list of the documents listed by the applicant was generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Patent literature cited

• WO 2005/071043 A1 [0002]
• DE 10356245 B4 [0002]

Claims (23)

Plant (1) for the catalytic production of diesel oil (9) from a starting material (7) from the group of residues, such as plastics (PE, PP, PET, PVC, etc.), cellulose-containing substances and / or biomaterials, comprising at least one feed system (100) for the starting material (7), a reaction unit (10), at least one one-part or multi-part separating and separating unit (3) and at least one sediment processing stage (200) for solids and / or sediments, the reaction unit (10) at least a reactor (11) for treating a mixed phase of a liquid carrier phase (carrier oil) and the solid starting material (7), the reactor (11) comprising at least one heating device (22) or a heating device (22) directly adjacent to this, and wherein the reactor (11) in normal operation has a gas or steam-filled head space (11.1) and a product space (11.2) filled with the mixed phase, comprising an inlet (12) for the starting material (7), a Head outlet (13) for a gas or vapor phase, an outlet (14) which is connected to a sediment processing unit (200) and at least one motor-driven agitator (15) for homogenizing and circulating the reactor contents, which is connected to at least one agitator (16) the product space (11.2) protrudes, the sediment processing unit (200) for discharging and separating solid contents from the product space (11.2), a conveying unit (61), a sedimentation vessel (60), a vertically below the sedimentation vessel (60) or close to the bottom in the sedimentation vessel (60) comprises a diverting element (63) arranged as a scratching or grinding conveying means, in particular as a screw conveyor, for the removal of residues containing oil and solids, characterized in that the sedimentation boiler (60) has a motor-driven transport element which is used as a scratching or scraping conveyor is formed, such as. A conveyor screw (62), is connected to the return inlet (23) of the reactor (11), which essentially forms the return line (23.1). Appendix (1) Claim 1 , characterized in that the motor-driven transport element is a return screw (62) which is connected in the upper third of the sedimentation vessel (60) to the latter and / or flanged directly to it. Appendix (1) according to one of the Claims 1 or 2 , characterized in that the motor-driven transport element (62) is sealingly connected to the end remote from the sedimentation vessel (60), and in particular the motor-driven transport element (62) from the sedimentation vessel (60) to the reactor (11) in the conveying direction Has a gradient which is inclined to the horizontal by the angle β, in particular is inclined by an angle β of 10 ° to 45 °. Plant (1) according to one of the preceding claims, characterized in that the sedimentation vessel (60) has a motor-driven scraping and scraping element (64). Plant (1) according to one of the preceding claims, characterized in that the sedimentation boiler (60) is connected to a coupling and purification unit (400), which in particular is a drying and evaporation unit, via the discharge element (63), especially a sludge conveyor screw for oily residues and a separation unit for steam and / or gas constituents. Appendix (1) Claim 5 , characterized in that a return line (23.1, 62) is provided from the drying and evaporator unit and / or the separation unit, which with at least one inlet on the reactor (11) and / or on the transport element (62), which is from the sedimentation boiler ( 60) leads to the reactor (11) is connected. Plant (1) according to one of the preceding claims, characterized in that the reactor (11) has a motor-driven rotary cutting unit (18) for the percussive and / or cutting comminution of the starting material (7), wherein a) the cutting unit (18) has at least one cutting edge or a cutting section (18.1) and is attached to and driven by the same drive shaft (17) as the at least one stirring body (16, 16.1, 16.2) and / or b) the at least one stirring body (16) as a cutting edge or is formed with a cutting section (18.1) or c) the cutting mechanism (18) has a drive shaft (20) and its own drive (21) independent of the drive (19) of the stirring unit (15). Plant (1) according to one of the preceding claims, characterized in that the drive (19) enables the speed of the stirring unit (15) of at least 400 to 500 rpm, advantageously enables a rotation of 440 to 470 rpm and / or a circumferential speed of the agitator (15) of 10 to 20 m / s can be achieved, ideally a circumferential speed of 13 to 18 m / s can be achieved .. Plant (1) according to one of the preceding claims, characterized in that the one-part or multi-part separation and separation unit (3) comprises at least one condenser (5) and / or a distillation column (4) for separating the diesel oil (9). Appendix (1) Claim 9 , characterized in that downstream of the reactor (11) the separation column (4) and subsequently the at least one condenser (5), ideally two condensers (5.1, 5.2), are arranged. Appendix (1) Claim 9 or 10 , characterized in that the separation column (4) forms a structural unit with the reactor (11) and is attached directly to the head space (11.1) or is connected to it. Plant (1) according to one of the preceding claims, characterized in that the reactor (11) comprises a heating device (22) which is designed to heat a filled mixed phase to between 200 ° C, ideally between 280 ° C and 320 To reach ° C. System (1) according to one of the preceding claims, characterized in that the heating device (22) is at least one microwave heater (22.1), and the at least one microwave heater (22.1) in particular has a power of 80 to 200 KW or more, and which of Product space (11.2) of the reactor (11) or the mixed phase leading, circumferential line (58) is separated by at least one pane, window and / or pipe made of glass or quartz glass. Appendix (1) Claim 13 , characterized in that the at least one microwave heater (22.1) comprises a safety lock (36) as a waveguide section which has an interior space (36.1) that can be evacuated, in particular an interior space (36.1) on which glass or quartz glass panes (36.2, 36.4) are arranged on both sides are. Plant (1) according to one of the preceding claims, characterized in that the reactor inlet (12) is shaped in such a way that a housing (26) of a screw conveyor (25) is held and sealed on it, in particular can be flanged directly to it. Plant (1) according to one of the preceding claims, characterized in that a supply unit for auxiliary and process media (8) is provided, which is connected to the reactor (11) by lines. Plant (1) according to one of the preceding claims, characterized in that the reactor (11) comprises at least one ultrasonic emitter, wherein the at least one ultrasonic emitter (33) is arranged in particular in the region of the product space (11.1). Process for the continuous production of diesel oil from a starting material (7) from the group of residual materials, such as plastics (PE, PP, PET, PVC, etc.), cellulose-containing materials (sawdust, shredded material) and biomaterials, which are converted into a liquid as a granular solid phase Phase is introduced from a carrier oil and catalytically transformed, characterized in that a system (1) according to one of the previous Claims 1 to 17th is provided, and where - the temperature in the mixed phase is between 200 and 400 ° C, ideally between 280 ° C and 350 ° C and - the mixed phase continues to have a proportion of lime of 1.5% to 10% by weight ( 2-5) and a proportion of catalyst of 1% by weight to 15% by weight (2-10), and wherein - the gaseous or vapor phase is continuously withdrawn from the head space (11.1) and downstream by means of at least one vacuum pump of the reactor (11) in at least one condenser (5) the diesel oil (9) is separated from the volatile gaseous or vapor phase. Procedure according to Claim 18 , characterized in that the starting material (7) contained in the mixed phase is mechanically comminuted by means of the at least one cutter or the cutting section (18) in the reactor (11). Method according to one of the Claims 18 or 19th , characterized in that the catalyst is a bentonite or zeolite, especially an aluminum silicate. Method according to one of the Claims 18 to 20th , characterized in that the peripheral speed of the agitator unit (15) is between 8 and 20 m / s, ideally between 13 and 17 m / s. Method according to one of the Claims 18 to 21st , characterized in that the pressure in the head space (11.1) of the reactor (11) is less than or equal to 1 bar, ideally in the range from 25 to 60 mbar. Method according to one of the Claims 17 to 21st , characterized in that a portion of the mixed phase is removed at the bottom outlet (14) and fed to a sedimentation tank (60), and the upper phase is returned directly from the sedimentation tank (60) by means of a scraping or scraping conveyor, in particular a return screw conveyor (62) is directed.

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