WO2019038276A1

WO2019038276A1 - Device and method for catalytic and/or pressureless oiling

Info

Publication number: WO2019038276A1
Application number: PCT/EP2018/072545
Authority: WO
Inventors: Karl Morgenbesser; Nikolaus SCHMIDT-OTT; Thorsten NEUKAMM
Original assignee: Karl Morgenbesser
Priority date: 2017-08-23
Filing date: 2018-08-21
Publication date: 2019-02-28

Abstract

Device for catalytic and/or pressureless oiling having an input system for input material, such as organic substances or plastics, having a reaction vessel, having a heat exchanger, and having a speed-regulated circulating pump, wherein the temperature in the reaction vessel is regulated by way of the input of heat, wherein the circulating pump is monitored for cavitation, and wherein the volumetric flow downstream of the circulating pump can be throttled by way of a throttle point.

Description

Apparatus and method for catalytic and / or pressure-free treatment

The invention relates to a device and a method for catalytic and / or pressure-less VERÖlung with an entry system for entry material, such as organic materials or plastics, with a reaction vessel, preferably a heat exchanger and a variable-speed circulation pump, wherein the temperature in the reaction vessel can be regulated by heat input.

Such systems are described in EP 1 538 191 B1 and in DE 10 2010 018 320 A1 as well as in DE 10 2010 100 606 75 B4 and WO 2016 1 16484 A1. In EP 1 538 191 A1, a system is shown in which in a circuit of the energy input for the depolymerization of a reaction mixture by means of a pump which promotes in a counter-rotating agitator, should take place. By such a stirrer can not or only to an insufficient extent be brought about a reduction or mixing of the respective reaction mass with the respective carrier oil. Although the chemical process of the catalytic pressure-free treatment is not called into question, the systems described in the cited documents correspond to a target concept and are not sufficiently developed in practice in your process management. According to a commissioned by the U.S. Army conducted study on a KDV

Pilot plant has been able to achieve a material throughput of no more than 20% of the target figure, and this only for a short period of time (Final Report / Excerpt, Ref Fuel AlphaKat Demonstration Program, December 2012, Covanta Renewable Fuels, LLC, Cooperative Agreement No. W9132T-09 -2-0024). Furthermore, from the report "State of the art for alternative methods for the thermal disposal of waste" of the Federal Environment Agency, D-06844 Dessau-Rosslau, Wörlitzerplatz 1, project number 29217 UBA-FB 002102, March 2017, chapter 2.3.2, 3.4 and 6.4 "Oilification processes claim to produce certain product fractions from certain waste fractions - usually comparable to fuel oil or diesel." Large-scale plants for the production of fuel oil or diesel in continuous operation do not yet exist In addition to the cost-effectiveness, proof of smooth continuous operation in weeks and months is still to be provided. "

From their own point of view, the previous systems are insufficiently monitored, controlled and regulated. Individual delivery units such as "friction turbines" (multi-chamber mixing systems, circulating pumps) are exposed to operating conditions that lead to cavitation and damage in the units.

It becomes dangerous when the cavitation becomes too violent; triggered, for example, by a faulty operation or by a reduction of the inlet pressure, for example by instability in a connected vacuum system. Heavy cavitation can reduce the flow to zero. The entire energy introduced by the engine is now distributed to the small volume of fluid within the pumping unit, resulting in a massive local temperature increase within seconds / minutes. This is not immediately apparent to the operator and does not lead to an automatic stop of the energy input. In connection with the medium at high temperatures, there is a risk that dangerous toxic substances such as dioxins, hexanes, furans, etc., form. The previously known feed systems for the reaction vessels work inadequately and thus make it difficult to stabilize the temperature in the reaction vessel. The condensation systems in the previously known KDV plants work inadequately, which is indicated by an increase in the pressure and the temperature in the reaction vessel and prevents undisturbed, stable outgassing.

No CT system is known which operates continuously and achieves the theoretically expected yield.

Against the background set out above, the present invention has the object underlying to provide a device for catalytic and / or pressure-free oiling, which can be operated with increased safety and improved yield. Likewise, the task was to specify a corresponding method. The invention has the particular object to eliminate the above-mentioned disadvantages and to operate stable and continuously with the indicated components KDV systems; This results in a result which almost corresponds to the theoretically expected yield and ensures that no toxic substances can be produced even in the case of operating errors or system malfunctions.

With respect to the device, this is done with the features of claim 1. A corresponding method is the subject of claim 47.

The present invention specifically uses the outside of the circulation pump P2 destructive and process-supporting acting properties of cavitation. Likewise, a comparable effect can be achieved by a crushing device. By such a shredding device can in particular a comminuting effect and optionally also an improved mixing can be achieved.

The dependent claims represent further advantageous embodiments of the device according to the invention, in particular the KDV system, as well as of the method according to the invention.

According to a preferred embodiment, the device is equipped with a subsequent to the reaction vessel condensation device.

According to a further preferred embodiment, the device is equipped with a subsequent to the reaction vessel distillation device K2. The distillation device K2 can be arranged between the reaction vessel and the condensation device.

More preferably, the temperature in the reaction vessel can be controlled by heat input by means of a heat input device. The temperature in the reaction vessel can optionally be regulated by heat input by means of electric heating and / or heat exchanger and / or circulating pump. In this way, the heat input can be controlled precisely and with little technical effort.

Furthermore, it can be installed to detect cavitation in the circulation pump in this a temperature measurement.

In order to detect cavitation in the circulation pump P2, a temperature measurement T2 can preferably be installed in the latter and a further temperature measurement T6 can be installed in the conduit 8, which are monitored for difference 53. The temperature T2 can be monitored at maximum 55 to automatically activate a shutdown of the power supply. According to one embodiment, the temperature T2 be monitored to a maximum of 55 to automatically activate a pre-alarm and on further increase a shutdown of the power supply, in order to reliably prevent the formation of toxic substances. A further advantage is that the measurements and / or measures for preventing cavitation in the circulating pumps can be carried out according to different measuring methods and / or methods.

More preferably, the throttle body be adjustable. Likewise, the throttle point can be axially flowed through and / or through which the risk of damage to the throttle can be reduced.

More preferably, the pressure behind the circulation pump P2 by adjusting the throttle D2 be adjustable. The pressure 61 behind the circulation pump P2 can be adjusted by adjusting the throttle D2 in order to expand the control range for energy input by the circulation pump P2 in the direction of lower energy.

Further preferably, the volume flow and / or the pressure downstream of the circulation pump P2 through the throttle point D2 be throttled and / or adjustable so that behind the throttle point D2 cavitation occurs, in particular by mixing and / or comminution and / or outgassing support.

It may also be advantageous if the inlet height H2 is selected to be so high for the speed-regulated circulating pump P2 that no cavitation occurs in the circulating pump P2 over the entire speed range. In particular, it may be advantageous if the inlet height H2 is selected to be so high for the speed-regulated circulating pump P2 that cavitation does not occur during undisturbed suction conditions in the circulating pump P2 over the entire speed range. It may also be advantageous if the circulation pump P2 is monitored for cavitation and / or is set up to automatically switch off the energy supply in good time before a critical process temperature is exceeded, in particular in order to prevent the formation of toxic substances.

Another embodiment is that the entry into the reaction vessel B2 by an adjustable feed system P3, with which the mass flow and / or flow is adjustable. The mass flow and / or volume flow may preferably be precisely adjustable with the adjustable feed system. This may have the advantage that the predetermined mass flow of feedstock E2 is accurately maintained, and thereby also the other feed systems for catalyst and neutralizing agent, e.g. the pumps P4, P5 are adjustable in a fixed and exact ratio to it.

It may also be advantageous if, by means of the adjustable feed system, the volume flow is adjustable independently of the pressure in the reaction vessel and the pressure upstream of the feed system. More preferably, the delivery system can be designed as a variable-speed volumetric pump. Furthermore, the feed system can be designed as a pump with a downstream control valve, which is preferably controlled by a flow controller. By using a variable speed volumetric pump P3 in

Combined with variable-speed volumetric feed pumps P4, P5, the ratio of the flow rates can be given by a fixed speed ratio. Only the use of a variable-speed volumetric pump for entry into the reaction vessel allows continuous operation with a significantly simplified control. According to a further embodiment, the reaction vessel B2 can be preceded by a storage tank B1 filled with carrier oil. The reaction vessel B2 may preferably be preceded by a feed tank B1 filled with carrier oil and connected to a circulation pump P1. The reaction vessel B2 and / or the storage tank B1 and, if necessary, a shredding device Z2 can be connected upstream. Finally, a metering device, in particular a speed-controlled conveyor screw, introduce entry material. The circulation pump P1 of the storage tank B1 can mix and / or heat the feed material E2, wherein the water content can evaporate. The use of a reservoir B1 with circulation pump P1 and crushing device Z2 makes it possible to optimally prepare the entry material E2 for further processing in the reaction vessel. The feed material E2 can be comminuted, mixed with carrier oil, heated to the evaporation temperature for water and then dehumidified. The comminution device Z2 homogenizes the entry mass E2, enlarges the surface of the solid particles involved in the reaction and thus accelerates the process.

Further, by throttling with the throttle D2, the pressure 61 behind the pump P2 can be set so high that cavitation occurs behind the throttle D2. In addition, cavitation of different intensity behind throttle D2 can be generated by targeted throttling downstream of pump P2. At this point, cavitation does not have a destructive effect, in particular not destructive on the pump P2, but supports the process with regard to mixing, comminution and evaporation / outgassing.

More preferably, in each case an analog level measurement L1 and L2 can be set up in the reservoir B1 and / or in the reaction vessel B2 over the entire vessel height. For both containers B1 and B2, control-relevant level states can be adjustable in order to serve as a control criterion. An advantage the level measurement defined in the reservoir B1 and the reaction vessel B2 is that minimum, maximum and operating levels can be formed and processed control technology. According to a further embodiment, in each case a redundant temperature measurement T3, Τ3 'in the feed tank B1 and / or in the reaction tank B2 below the minimum level L1 1, L21; T4, T4 'be mounted, in particular in order to act as an actual value for acting on the speed adjustment of the circulation pump temperature control. The temperature measurement in container B1, B2 can have a high priority for the reliability of the system, which is why it can be redundant and processed in a selection circuit, which also takes extreme values, as the actual value of the temperature control acting on the speed adjustment of the circulation pump P1, P2 temperature control can be. For detecting cavitations of the circulation pump P1 and / or the circulating pump P2, an empirically determined curve 50, 51 may each exist. In the curve, the electrical drive power of the pump P1, P2 can be represented as a function of their speed during normal operation, in order to detect with a negative deviation cavitation of the pump P1, P2 in a further way. Likewise or alternatively, in the curve, the electrical drive power of the pump P1, P2 may be represented as a function of their speed during normal operation to have a positive deviation signal and / or an indicator for the accumulation of non-evaporable solids available. It may therefore be advantageous to have a further independent measurement, with the cavitation of the circulation pumps P1, P2 can be seen and at the same time for the container B1, B2 provides an indication of the proportion of solids, if appropriate, to ablate a portion of Umwälzmenge and by To replace fresh oil.

More preferably, the throttle bodies D1, D2 can be configured as a single nozzle or individual diaphragm or from a plurality of switchable nozzles or diaphragms. It It may be advantageous to adapt the type and number of nozzles to the feed material and to the volume flows.

Subsequent to the throttle point D2 of the reaction vessel B2, a straight pipe section 21 with a length greater than the length of a cavitation jet forming therein can be present in an advantageous manner. The inner wall of the straight pipe section 21 may have a sufficient lateral distance to the cavitation after the throttle point D2. Advantageously, behind the throttling point D2, a tube piece 21 that is as long as possible (at least 1 m) can prevent harmful effects of cavitation.

The system or device can be advantageously equipped with a combined heat and power plant CHP, which is preferably also operable with the fuel obtained from the system and / or at various points B3, B4, B5, B6, K4, K5 in the system and / or device inevitably evacuated and not further processed vapors sucks and burns. This results in an elegant way to feed inevitably resulting and not further processed vapors into the intake pipe of the cogeneration unit CHP and make harmless by combustion.

More preferably, the combined heat and power plant CHP can be operated instead of a gas engine M with a gas turbine, which preferably emits heat energy at a higher temperature level. The use of a gas turbine in a CHP can provide the advantage that the heat energy delivered is available at a higher temperature level and that thus the heat exchangers acted upon can be made smaller. Only the high temperature level of a gas turbine makes it possible to realize heating tasks in the temperature range of the reaction vessel B2. According to a further embodiment, reservoirs B3, B4 may be present, which are preferably both heatable with energy from the combined heat and power plant CHP. A reservoir B3 can be maintained at a temperature below the boiling point of water via the heat exchanger W3. The other reservoir B4 can be kept below the reaction temperature of the current feed E1 via the heat exchanger W4. This can have the advantage that the operating temperature in the storage tank B1 and B2 in the reaction vessel is achieved faster by the supply of preheated oil from the storage tanks B3, B4.

It may also be advantageous if the temperature in the reaction vessel B2, as long as no product is added, in addition to the energy input by the circulation pump P2 and / or by the electric heater EH2 and by the heat exchanger W2, which is integrated into the suction line 7 and / or is supplied with the high-temperature waste heat of the combined heat and power plant CHP is affected.

More preferably, the volumetric pump P3 in the suction line 7 of the circulation pump P2 feed a predetermined amount before the heat exchanger W2, which was previously decoupled by closing a valve V10 from Umwälzkreislauf. For circulating a strand 9 can be connected by opening a valve V1 1 parallel to the heat exchanger W2.

It is also possible, as long as the volumetric pump P3 promotes to regulate the outlet temperature T9 of heat exchanger W2 as a function of the current temperature T4, T4 'in the reaction vessel B2 by supplying heating energy through valve V7.

It may result in an advantage that the content in the reaction vessel B2, in addition to the energy input by the circulation pump P2, and by one of the high temperature of the cogeneration unit CHP powered heat exchanger W2 can be heated and thereby the achievement of the reaction temperature can be accelerated. After reaching the operating temperature in the reaction vessel B2 switching takes place via valves V10, V1 1, V12, which strömström the liquid Ström from the reaction vessel B2 on the heat exchanger W2 and that now product from the feed tank B1 during transfer to the reaction vessel B2 in this heat exchanger W2 is brought to approximately the operating temperature of the reaction vessel B2, which is advantageous for the regulation of the operating temperature in the reaction vessel B2.

According to a further embodiment, both catalyst and neutralizing agent, preferably in a known ratio mixed with carrier oil, may each be contained in a storage tank B5, B6. Preferably, both catalyst and neutralizing agent, preferably in a known ratio mixed with carrier oil, in each case be contained in a storage tank B5, B6, there mixed with agitator R1, R2 and / or permanently mixed and / or each with a variable speed Volumetric pump P4, P5 be introduced into the suction line of the circulation pump P2. The pumps P4, P5 can preferably be controllable in a dependent relationship to the rotational speed of the pump P3. It may be advantageous to keep in storage tanks B5, B6 catalyst or neutralizing agent in a known mixture and deliver in a dependent on the output amount of the discharge pump P3 ratio in the reaction vessel B2, this ratio is controlled by the ratio of speeds. This allows accurate and control technology simple dosing.

According to yet another embodiment, a differential pressure measurement 76, 66 between pressure in the dome of the container B1 and / or container B2 and atmosphere may be appropriate. The differential pressure measurement can serve as an actual value for a pressure regulator 78, 67 which controls the condensation K1, K3 at the outlet of the container B1, B2 and monitors for deviation in both positive 69 and negative 68 direction. This is preferably done via an alarm disturbances in the condensation K1, K3 display and / or large positive deviation to stop the power supply by pump P1 and / or pump P2 and heat exchanger W1 and / or heat exchanger W2 and / or material flow through pumps P1 , Z1, Z2, P6 and / or pumps P3, P4, P5 to interrupt. It may be advantageous to measure the differential pressure to the atmosphere in the dome of the reaction vessel B2 and storage vessel B1 in order to keep it constant for stable operation and to signal disturbances in the condensation in the event of deviations and if there are excessively large amounts of energy and energy Stop material supply automatically.

According to a further embodiment, a common container 90 can be used for collecting both the condensed process water and the auskonden- centered distillate. The level can be measured with two float level measurements 91, 92. Furthermore, the floats 93, 94 may be designed for different densities. The level of the lighter middle distillate can be computationally corrected with the level of the heavier process water. The level versus time waveform can be an important indicator of a) current yield (slope) and / or b) stability (continuity) of the overall process.

The above statements on the device according to the invention are also valid for the method according to the invention.

In the following the invention is shown by means of embodiments.

Show it: Fig. 1 a, 1 b, 1 c, 1 d schematically an embodiment diagram for the construction of a system according to the invention.

2a, 2b, 2c schematically characteristic curves for the process control, which are derived from the characteristic diagram of a circulating pump for different throttle positions at constant pump pressure.

Fig. 3 shows schematically an adjustment characteristic, which results from the characteristics of Fig. 2a, 2b, 2c and serves as a basis for the adjustment of the throttle D1, D2.

Fig. 4 shows schematically for a circulation pump in a power-speed diagram an empirically determined curve for the operation and limits for deviations, which represent too high a degree of solids loading or a typical power loss in cavitation.

Fig. 5 shows schematically a drive logic of the circulation pump P1. Fig. 6 shows schematically a drive logic of the circulation pump P2. In the figures 1 a, 1 b, 1 c, 1 d, an overall scheme for the construction of a KDV system according to the invention is shown, in the figure 1 a, a combined heat and power CHP, a low-temperature reservoir B3 and a high-temperature reservoir B4 are shown 1 b shows an entry system E 1 with storage tank B1, FIG. 1 c shows the actual reaction vessel B2 with subsequent evaporation column K2, and FIG. 1d shows a condensation system K3.

1 a shows a combined heat and power plant CHP with a motor M, a generator G for power generation, a low-temperature heat exchanger WT-NT and a a high-temperature heat exchanger WT-HT and a suction 80 with suction filter 81.

From the low-temperature heat exchanger WT-NT hot heat transfer oil is passed via pipe 16 to a heat exchanger W3 in a storage tank B3 and returned via pipe 15 again. From the high-temperature heat exchanger WT-HT hot heat transfer oil via pipe 30, 17 to a heat exchanger W1 (Fig. 1 b) out and returned via pipe 31, 18 again.

The reservoir B3 is filled with unloaded carrier oil, which is circulated with a stirrer 36 and is maintained at a temperature T7. From the dome of the reservoir B3 a suction line 23 leads to the suction 80th

With a discharge pump P6 10 carrier oil is passed through valve V6 and pipe into a feed tank B1.

A reservoir B4 is filled with carrier oil for high temperature, which is kept in motion with a stirrer 37 and is maintained at a temperature T8 by a heat exchanger W4, wherein hot heat transfer oil is fed via a pipe 34 to the heat exchanger W4 and returned via a pipe 35 again , From the container B4 also performs a suction 24 in the intake 80 of the cogeneration plant CHP. High-temperature carrier oil is fed from the reservoir B4 via a discharge pump P7 and pipe 12 into a reaction vessel B2 (FIG. 1c).

From the high-temperature heat exchanger WT-HT leads a pipe 30 with hot heat transfer oil to a heat exchanger W2 (Fig. 1 c) and back via pipe 31st In FIG. 1b, feed material E2 treated with a metering device Z1 in the form of a screw conveyor is fed via a pipeline 1 to a comminuting device Z2 and a circulating pump P1, the pump P1 being connected via a pipeline 2 to a restrictor D1 at the inlet of the receiving vessel B1 promotes and the liquid flow Q is continued in a straight pipe section 20 within the storage tank B1.

The company Vogelsang GmbH & Co. KG (DE, 49632 Essen / Oldenburg, Holthöge 10-14) has crushing plants in its assortment for plastics and other waste.

From the lower part of the container B1 leads a pipe 3 to the heat exchanger W1 and further via a pipe 4 in the suction line. 1

The storage tank B1 is equipped with an electric heater EH1, a sight glass S1 and an analog level measurement L1. From the upper part of the container B1 is a connection either in a Ausdampfleitung 26 or via pipe 1 1 in a condensation device K1, depending on the nature of the entry material E2 and the pollutants contained therein.

The throttle point D1 has an adjustable drive surface 64 with a passage surface, wherein the actuator 64 is driven by a pressure regulator 60, 62 to regulate the pressure 60 even at variable flow rate to a constant pressure. In addition, a temperature sensor T5 is mounted in a pressure line 2, which evaluates a differential temperature 52 in cooperation with a temperature sensor T1 in the pump P1 to detect cavitation of the pump P1 and turn off the pump P1, if necessary, automatically. In addition, there is a maximum monitoring 54 for the temperature sensor T1, also cavitation in to recognize the pump P1 and turn off the pump P1 if necessary automatically.

With the analogue level measurement L1, different levels are defined within the receiver B1, such as e.g. an adjustable maximum height L12 and an adjustable minimum height L1 1. The level in the storage tank B1 is controlled by pump P6 (FIG. 1a), which conveys warm carrier oil from the storage tank B3 (FIG. 1a), and control valve V6 is regulated via the pipe 10 to a constant value. For the measurement of the operating temperature in the liquid region of the receiver B1, a temperature sensor T3, T3 'is mounted, the signal of which is forwarded for various tasks.

The heat exchanger W1 is heated via the pipe 17 with hot heat transfer oil from the high-temperature heat exchanger WT-HT of the combined heat and power plant CHP (FIG. 1 a). The heating power is set via the control valve V5 in pipe 18. The temperature control for T3 in the storage tank B1 is carried out optionally via the heat exchanger W1 (circulation pump P1 adopts the base load at a constant speed) or via the circulation pump P1 (heat exchanger W1 uses the entire available energy of the combined heat and power plant CHP). In case of failure of the circulation pump P1, the valve V5 in the pipe 18 is closed immediately and the entry screw Z1 is stopped immediately.

A typical manufacturer of suitable heat exchangers and liquid condensers is Kelvion Holding GmbH (DE, 44809 Bochum, Dorstener Str. 484).

Before loading the receiver tank B1 with feed material E2, it is filled with warm carrier oil from the storage container B3 (FIG. 1a) to a minimum level L1. Only then is the entry material E2 via the entry screw Z1 introduced and the comminution Z2 and circulating pump P1 supplied. With the heat exchanger W1 and the energy input through the circulation pump P1, the medium in the storage tank B1 is heated to such an extent that the water present in the feed material E2 evaporates.

The level in the reservoir B1 is kept constant by controlled introduction of unloaded carrier oil from the reservoir B3 (Figure 1a) via pump P6 (Figure 1a), valve V6 (Figure 1a) and line 10. At minimal load of the carrier oil with solids in the reservoir B1 empirically a characteristic 50 "drive power N over speed n" was determined. Deviations of the operating point from this characteristic 50 (Figure 4) are a measure of the degree of solids loading. If a limit value is exceeded, the loaded carrier oil is drained via a valve V13 and fed to an external processing plant. Subsequently, container B1 is filled up again from storage container B3 (FIG. 1a) with unloaded carrier oil.

Systems of this type are usually operated via a freely programmable control with user interface, visualization and data recording (Prozessleit- system 79). In addition to the usual data recording of a process control system 79, another Datalogger 79a is installed especially for diagnostics and fault value analysis in which all available analogue and binary information is stored via bus from the controller with a high temporal resolution (<100 msec).

A typical manufacturer of a corresponding diagnostic system is the company Delphin Technology AG (DE, 51427 Bergisch Gladbach, Lustheide 81), which in addition to the usual data logger software with numerous tools for diagnosis and fault analysis offers. In Fig. 1 c, a distillation column K2 and the reaction vessel B2 are shown, which is supplied from the pump P3 (Fig. 1 b) via the pipe 5, wherein the conveyed amount first passes through a check valve V12 in a pipe 6 and through the Heat exchanger W2 leads into a suction line 7 for the circulation pump P2, which feeds on its pressure side in a pipe 8. Pipe 8 leads via a throttle point D2 and pipe 21 to the inlet of the reaction vessel B2. The throttling of D2 can be varied with a pressure measurement 61 with a pressure regulator 63 via an actuator 65 to adjust the pressure before throttle D2 and thus the intensity of the cavitation after throttle D2.

Schubert & Salzer Control Systems GmbH (DE, 85053 Ingolstadt, Bun- senstr. 38) has slide gate valves in its range which are suitable for such an application. At initial filling of the reaction vessel B2 carrier oil from the high-temperature storage tank B4 (Fig. 1 a) with pump P7 (Fig. 1 a) is entered via line 12 until reaching a minimum operating level L21 in the reaction vessel B2. Once a level is exceeded in the container B2, which prevents the dry running of the pump P2, this can be started. The circulation in the container via a valve V10 in the line 6, the heat exchanger W2, the line 7, the circulation pump P2, the line 8, the throttle D2 and the tube 21; the valves V1 1 and V12 are closed. With the beginning of the transfer process via the pump P3, the valve V12 is opened in the line 5, the valve V10 is closed in the line 6 and the valve V1 1 is opened in a line 9. By opening the valve V1 1, the heat exchanger W2 is bypassed for the recirculation. The feed material is passed through the heat exchanger W2 and regulated via a valve V7 in a line 31 to the temperature in the reaction vessel B2. Setpoint of this temperature control is a temperature T4 in the reaction vessel B2. Actual value is a temperature T9 behind heat exchanger W2. The actuator of the control loop is a valve V7 in the line 31st High-temperature circulating pumps are produced, for example, by Allweiler GmbH (DE, 78315 Radolfzell, Allweilerstr. The reaction vessel B2 is additionally equipped with an electric heater EH2. Through a sight glass S2, the level in the container B2 can be observed in order to recognize the intensity of the evaporation process and any foaming can. The reaction vessel B2 also has an analogue level measurement L2, with the level switching points, such as an adjustable maximum height L22 and an adjustable minimum height L21, can be fixed.

A temperature T2 within the pump P2 is monitored for difference to the temperature T6 in line 8. The exceeding of a limit value 53 is interpreted as cavitation and activates the switching off of the pump P2.

In addition, the temperature T2 in the pump P2 is monitored to a maximum value 55. The exceeding of the limit value 55 is interpreted as cavitation of the pump P2 and leads to the shutdown of the pump P2.

With the switching off of the pump P2 and the discharge pump P3 is stopped and the temperature control valve V7 to the heat exchanger W2 closed.

Parallel to the transfer via discharge pump P3, neutralization agent is fed from a reservoir B5 catalyst via a volumetric pump P4 and the line 12 and from a reservoir B6 via a volumetric pump P5 and via a line 13 into the suction line 7 of the circulation pump P2.

In the reservoir B5 carrier oil and catalyst are mixed in a predetermined ratio and are maintained by a stirrer R1 in their mixture. The speed of the feed pump P4 is dependent on the speed of the discharge pump P3 to feed the exact amount of catalyst for the charged solid. The speed of the feed pump P5 is dependent on the speed of the discharge pump P3 to feed the exact amount of neutralizing agent for the input solid.

Resulting gases in the containers B5 and B6 are sucked off via a line 27 to the combined heat and power plant CHP.

When the level in the tank B2 has reached the maximum value L22 or when a curve 51 indicates a high solid load, the transfer operation is stopped (stop the discharge pump P3 and close the valve V7) and the level in the tank B2 by discharging through a valve V14 up to lowered to a minimum operating level L21 in an external treatment plant.

A constant pressure in the dome of the container B2 is a prerequisite for a stable process. The differential pressure to the atmosphere is measured by a differential pressure transmitter 66 and serves as an actual value for a control of the condensation. In addition, the value is still monitored for a minimum limit value 68 and a maximum limit value 69, the maximum limit value 69 stopping the energy supply by switching off the circulation pump P2. Fig. 1 d shows an air condenser K3, in which the resulting vapor via a pipe 22 enters and condenses here to liquid (middle distillate). A control 67 of the head pressure in the container B2 acts on the speed adjustment of an air condenser K3. Via a pipe 29 and a siphon 96, the condensate is fed into a collecting tank 90 for middle distillate. The receiver 90 is equipped with two different density based analog float level measurements 91/93, 92/94. The float 93 is designed for the density of water, the middle distillate density float 94. Both levels 91, 92 are monitored for minimum and maximum limits 97/98, 99/100, activate the discharge valves 101, 102 to discharge water or middle distillate into a water tank K4 and a middle distillate tank K5, respectively. Gases forming in the tanks K4, K5 and 90 are collected via a line 25 and extracted by the cogeneration unit CHP (FIG. 1 a).

FIG. 2 a schematically shows pump characteristics for different rotational speeds n for circulating pumps P 1, P 2 in a rotational speed range from n MIN to n MAX. In addition, various throttle characteristics s1, s2, s3 for the variable throttles D1, D2 are shown. The intersection of the throttle characteristic s4 (throttle D1, D2 fully open) with the maximum speed characteristic n-MAX shows the operating point 1 10 for maximum energy input. Each pressure 60, 61 before the throttle point D1, D2 corresponds for each speed of a specific throttle position D1, D2. In Fig. 2b, the power requirement for different rotational speeds of the circulation pumps P1, P2 is shown schematically. The dot-dash line corresponds to the power requirement at constant pressure 60, 61, which represents the possible energy input within a speed control range 59. The adjustable pressure 60, 61 in front of the throttle points D1, D2 is decisive for the intensity of the cavitation after the throttle points D1, D2. 109 indicates the variable energy input without adjustable throttle; 59 identifies the significantly larger variable energy input with adjustable throttle. 2c schematically shows the adjustment path of the adjustable throttles D1, D2 over the flow rate at different forward pressures 60, 60 ', 60 ", 61, 61', 61". From FIGS. 2a, 2b, 2c, a diagram according to FIG. 3 results, in which the adjustment path of the throttle D1, D2 is plotted over the rotational speed n of the pump P1, P2. The characteristic acc. Fig. 3 is stored in a process control system 79, so that the position of the throttle D1, D2 is set depending on the rotational speed n and thus ensures a stable control.

FIG. 4 shows an empirically determined curve 50, 51 as well as a limit curve 72 ', 72 "for solids loading and a limit curve 71', 71" for cavitation in the pump P1, P2. The curve 50, 51 shows the drive power of the pump P1, P2 at operating temperature as a function of the rotational speed n at minimum load of the carrier material with solids and at a predetermined pressure 60, 61 before throttle D1, D2 for cavitation behind throttle D1, D2. Operating points 74 ', 74 "above the reference curve 50, 51 are a measure of the loading of the carrier material with solids. Operating points 73', 73" below the reference curve 50, 51 are an indicator of cavitation in the pump P1, P2.

If the operating point 73 ', 73 "is undershot, the pump P1, P2 is automatically switched off The operating point 50', 51 'is the theoretical operating point at minimum solids loading , which should be counteracted by brief interruption of the entry via pump P3 and the energy supply via valve V7 and lowering the level to the minimum level L21 via the discharge valve V14. 5 schematically shows a logic module for controlling the circulating pump P1 in a process control system 79. In the upper area are relevant analog signals, in the lower area relevant binary signals are shown.

All analog signals, which cause an adjustment of the speed n of the pump P1, are connected to a logic device, the MIN selection 105. The signal that calls for speed reduction, is switched through to the speed adjustment of the pump P1.

For the reservoir B1 each four analog signals are interconnected: differential pressure measurement 76, temperature measurement T3, level measurement L1 and manual adjustment 84 for the speed n of the pump P1.

In normal operation, the temperature controller T3. When starting the system, the storage tank B1 is not yet filled. The pump P1 is switched on as soon as the MIN level for dry running protection 86 is exceeded. Now the level controller L1 engages and reduces the speed n and thus the flow rate to a value at which an overshoot of the oil jet is excluded in the upper part of the reservoir B1. After exceeding level L1 1, the temperature controller T3 takes over and increases the speed to n-MAX until the setpoint of T3 is reached.

All digital signals causing a stop of the pump P1 are linked in the process control system 79 via an AND module 107: pressure dP-MAX 77, temperature T-MAX 54, level 86, temperature difference 52, emergency stop 88manual OFF 103 and power loss 73 'of the pump P1.

The wiring of the stop criteria is designed to be break-proof; If only one of these contacts changes to the ZERO state, the pump is stopped. 6 schematically shows a logic module for controlling the circulating pump P2 in a process control system 79. In the upper area are relevant analog signals, in the lower area relevant binary signals are shown. All analog signals that cause an adjustment of the speed n of the pump P2 are connected to a logic device, the MIN selection 106. The signal requesting speed reduction is switched to the speed adjustment of the pump P2. Four analog signals are connected in each case for the reaction vessel B2: differential pressure measurement 66, temperature measurement T4, level measurement L2 and manual adjustment 85 for the rotational speed n of the pump P2.

In normal operation, the temperature controller T4. If it comes, for example, by a disturbance in the condensation K3 to a pressure increase 66 in the reaction vessel B2, so the speed adjustment is bumpless and instantaneous on the pressure controller 67 via. By this selection circuit 106 is also ensured that the speed n can also be moved manually only within the allowable limits n-MIN, n-MAX.

All digital signals that cause a stop of the pump P2 are linked in the process control system 79 via an AND module 108:

Pressure dP-MAX 69, temperature T-MAX 55, level 87, temperature difference 53, emergency stop 89, manual OFF 104 and power loss 73 "of the pump P2

The wiring of the stop criteria is designed to be break-proof; If only one of these contacts changes to the ZERO state, the pump is stopped.

By using two containers B1 and B2 in the system shown, their processes (comminution of the input material E2 and evaporation of water and the actual KDV method) can also be run independently of each other and combined in batch mode. The present invention generally also relates to a device and a method for catalytic and / or pressure-free treatment in a plant with an entry system for input material such as organic materials or plastics, with a reaction vessel, with a heat exchanger before the reaction vessel, with a speed-controlled circulating pump and a to the reaction vessel subsequent condensation device, wherein the temperature in the reaction vessel by heat input by means of electric heating and / or heat exchanger and / or circulating pump is controlled. If the operating point of the circulation pump slides off due to disturbances in the intake into the cavitation area, this is detected several times and the circulation pump and thus the energy supply are automatically stopped to prevent the formation of toxic substances. By throttling the pressure to the pump, the control range for the energy input through the circulation pump can be increased compared to pure speed control. By raising the pressure upstream of the throttle point, cavitation of varying intensity can be generated after the throttle point in order to support the reaction process, without the cavitation having a detrimental effect on this point. Only the use of a variable-speed volumetric pump for entry into the reaction vessel allows continuous operation with a significantly simplified control.

LIST OF REFERENCE NUMBERS

1 pipeline between entry system and shredding unit Z2

2 Circulation pump P1 to the adjustable throttle D1

3 pipeline reaction vessel and heat exchanger W1

4 Pipe heat exchanger W1 and entry auger

5 Piping transfer B1 to B2

6 Pipeline B2 to W2

7 Pipeline W2 to P2

8 Piping P2 to D2

9 Piping V1 1 to suction line 7 of P2

10 Pipeline Reservoir B3 to B1

1 1 Pipeline to the condensation device K1

12 Pipeline reservoir B4 to B2

13 pipeline storage tank catalyst to P4

14 Pipeline storage tank neutralizing agent to P5

15 return line to CHP WT-NT

16 Heating cable from CHP WT-NT

17 Heating cable from CHP WT-HT

18 Return line to CHP WT-HT

19 Fan of the air condenser K1

20 straight pipe section downstream of restriction D1

21 straight piece of pipe after throttle point D2

22 Pipeline to condenser K3

23 Suction line from B3

24 Suction line from B4

26 exhaust pipe

27 suction line

28 Fan of the air condenser K3

29 Fluid drain from the condenser K3 30 Heating cable from CHP WT-HT

31 Return line to CHP WT-HT

32 stop valve

33 shut-off valve

34 Heating cable from CHP WT-HT

35 Return line to CHP WT-HT

36 agitator in reservoir B3

37 Agitator in reservoir B4

38 shut-off valve

39 shut-off valve

40 shut-off valve

41 stop valve

42 shut-off valve

43 stop valve

44 shut-off valve

45 shut-off valve

46 shut-off valve

47 shut-off valve

48 shut-off valve

49 shut-off valve

50 curves Power over speed Pump P1

50 'operating point pump P1

51 curves Power over speed Pump P2

51 'Operating point pump P2

52 logic module "T1 -T5"

53 logic module "T2 + T6"

54 MAX monitoring T1

55 MAX monitoring T2

56 stop valve

57 shut-off valve 58 stop valve

59 Control range energy input with adjustable throttle

60 pressure measurement behind P1

60 'lowered pressure behind pump P1

60 "raised pressure behind pump P1

61 Pressure measurement behind P2

61 'lowered pressure behind pump P2

61 "raised pressure behind pump P2

62 pressure regulator P1

63 Pressure regulator P2

64 actuator for D1

65 actuator for D2

66 Differential pressure measurement tank B2

67 Pressure regulator for B2 over condensation

68 MIN limit pressure in B2

69 MAX limit pressure in B2

70 reference characteristic

71 'Limit curve for cavitation pump P1

71 "limit curve for cavitation pump P2

72 'Limit curve for solids loading Pump P1

72 "Limit curve for solids loading pump P2

73 'power loss pump P1

73 "power loss pump P2

74 'power increase pump P1

74 "power increase pump P2

75 Theoretical operating point

76 Differential pressure measurement tank B1

77 MAX limit pressure in B1

78 Pressure regulator for B1 via condensation process Control System

Data logger

Intake gas engine

Suction

Control characteristic for actuator 64

Control characteristic for actuator 65

Manual adjustment speed pump P1

Manual adjustment speed pump P2

Dry run protection container B1

Dry running protection container B2

Emergency stop pump P1

Emergency stop pump P2

Collection container middle distillate

level measurement

Swimmer water

Float middle distillate

siphon

MAX level of water

MIN level of water

MAX level middle distillate

MIN level middle distillate

Discharge valve water

Discharge valve middle distillate

Manual off / on pump P1

Manual off / on pump P2

Logic block for MIN selection pump P1

Logic block for MIN selection pump P2

Logic module AND pump 1 108 logic module AND pump 2

109 Control range energy input without adjustable throttle

1 10 Operating point for maximum energy input

B1 storage tank

B2 reaction vessel

B3 low temperature storage tank

B4 storage tank high temperature

B5 storage tank catalyst

B6 storage tank neutralizing agent CHP cogeneration plant

D1 Orifice at the inlet of tank B1

D2 choke point at inlet tank B2

E1 entry system

E2 Entry material EH1 Electric heater Reservoir B1

EH2 electric heating reaction tank B2

G generator

H1 inlet height to pump P1

H2 Inlet height to pump P2 K1 Condensing device for hopper

K2 distillation column (distillation device)

K3 Condenser for middle distillate

K4 water tank

K5 middle distillate tank L1 analogue level measurement

L2 analogue level measurement

L1 1 adjustable minimum height for operation

L21 adjustable minimum height for operation L12 adjustable maximum height for operation

L22 adjustable maximum height for operation

M engine

N power pump P2 or P1

n Speed pump P2 or P1

n-MIN Minimum speed pump P2 or P1

n-MAX Maximum speed of pump P2 or P1 n ^* Operating speed of pump P2 or P1

P1 Circulation pump Reservoir

P2 circulation pump reaction tank

P3 delivery system, volumetric pump

P4 entry pump catalyst

P5 Inlet pump neutralizing agent

P6 discharge pump container B3

P7 discharge pump container B4

Q delivery rate

R1 mixer tank B5

R2 mixer tank B6

S1 Sight Glass Reservoir

S2 sight glass reaction vessel

s1 valve lift at minimum operating speed s2 valve lift at medium operating speed s3 valve lift at cavitation pressure at max. Speed s4 valve lift 100%

T1 temperature sensor in the pump P1

T2 Temperature sensor in the pump P2

T3 Temperature sensor / regulator Reservoir B1

T3 'Temperature sensor / regulator Reservoir B1 T4 temperature sensorY-regulator reaction tank B2

T4 'Temperature sensor / controller Reaction tank B2

T5 temperature sensor in front of the throttle D1

T6 temperature measurement pressure line 8

T7 temperature sensor reservoir B3

T8 temperature sensor reservoir B4

T9 temperature sensor to W2

V5 temperature control valve to heat exchanger W1

V6 level control valve for storage tank B1 V7 Temperature control valve to heat exchanger W2

V10 shut-off valve

V1 1 shut-off valve

V12 shut-off valve

V13 Discharge valve Reservoir B1

V14 discharge valve reaction tank B2

W1 heat exchanger on the receiver B1

W2 heat exchanger at the reaction tank B2

W3 heat exchanger in storage tank B3

W4 heat exchanger in storage tank B4

WT-NT Low Temperature Heat Exchanger

WT-HT heat exchanger high temperature

Z1 metering device

Z2 shredder

Claims

claims

1 . Device for the catalytic and / or pressureless oiling with an entry system for input material, such as organic substances or plastics, with a reaction vessel (B2), preferably a heat exchanger (W2) and with a speed-controlled circulating pump (P2), wherein the temperature (T4) in the reaction vessel (B2) is controllable by heat input, characterized

that the circulation pump (P2) is monitored for cavitation and

the volume flow through a respective throttle point (D2) downstream of the circulation pump (P2) and / or downstream of a circulation tank (P1) upstream of a circulation pump (P1) can be throttled and / or is guided by a comminuting device (Z2, Z2 ').

2. Apparatus according to claim 1, characterized by a to the reaction vessel (B2) subsequent condensation device (K3) and / or characterized by a to the reaction vessel (B2) subsequent distillation device (K2) and / or characterized by a between the reaction vessel (B2) and a condensation device (K3) arranged distillation device (K2).

3. Apparatus according to claim 1 or 2, characterized in that the

Temperature (T4) in the reaction vessel (B2) can be regulated by heat input by means of a heat input device. Device according to one of the preceding claims, characterized in that the temperature (T4) in the reaction vessel (B2) is selectively controllable by heat input by means of electric heater (EH2) and / or heat exchanger (W2) and / or circulation pump (P2).

Device according to one of the preceding claims, characterized in that for detecting cavitation in the circulation pump (P2) in this a temperature measurement (T2) is installed.

Device according to one of the preceding claims, characterized in that for the detection of cavitation in the circulation pump (P2) in this a temperature measurement (T2) and in the conduit (8) a further temperature measurement (T6) are installed, the difference (53) are monitored.

Device according to one of the preceding claims, characterized in that the temperature (T2) in the circulation pump (P2) is monitored for maximum (55) to automatically activate a shutdown of the power supply.

Apparatus according to claim 6 or 7, characterized in that the

Temperature (T2), in particular the temperature (T2) in the circulation pump (P2), to maximum (55) is monitored to automatically activate a pre-alarm and further increase a shutdown of the power supply, in particular so as to reliably prevent the formation of toxic substances prevent.

9. Device according to one of the preceding claims, characterized in that the throttle point is adjustable and / or that the throttle point is axially flowed through and / or flowed through.

10. Device according to one of the preceding claims, characterized in that the volume flow and / or pressure behind the circulation pump (P2) through the throttle point (D2) is throttled and / or adjustable so that behind the throttle point (D2) cavitation occurs, in particular to thereby assist the mixing and / or comminution and / or outgassing.

1 1. Device according to one of the preceding claims, characterized in that the pressure (61) behind the circulation pump (P2) by adjusting the throttle (D2) is adjustable.

12. Device according to one of the preceding claims, characterized in that the pressure (61) behind the circulation pump (P2) by adjusting the throttle (D2) is adjustable to the control range for energy input through the circulation pump (P2) in the direction of lower energy expand.

13. Device according to one of the preceding claims, characterized in that the inlet height (H2) to the speed-controlled circulation pump (P2) is selected so high that in the circulation pump (P2) over the entire speed range no cavitation occurs and / or that the inlet height ( H2) to the speed-regulated circulating pump (P2) is so high that no cavitation occurs in undisturbed suction conditions in the circulating pump (P2) over the entire speed range.

14. Device according to one of the preceding claims, characterized in that the circulation pump (P2) is monitored for cavitation and / or is set up in order to automatically switch off the energy supply in good time before exceeding a critical process temperature. drove, in particular to prevent the formation of toxic substances.

15. Device according to one of the preceding claims, characterized in that the entry into the reaction vessel (B2) by an adjustable feed system (P3), with which the mass flow and / or volume flow is adjustable.

16. The device according to claim 15, characterized in that the mass flow and / or mass flow with the adjustable feed system (P3) is exactly adjustable.

17. The apparatus of claim 15 or 16, characterized in that the mass flow and / or flow through the adjustable feed system (P3) is independent of the pressure in the reaction vessel (B2) and the pressure upstream of the feed system (P3) adjustable.

18. Device according to one of the preceding claims, characterized in that the supply system is designed as a variable-speed volumetric pump (P3).

19. Device according to one of the preceding claims, characterized in that the feed system is designed as a pump with downstream control valve, which is preferably controlled by a flow control.

20. Device according to one of the preceding claims, characterized in that the reaction vessel (B2) is preceded by a filled with carrier oil storage tank (B1).

21. Device according to one of the preceding claims, characterized in that the reaction vessel (B2) is preceded by a feed tank (B1) filled with carrier oil with a circulating pump (P1). 22. The apparatus of claim 20 or 21, characterized in that the reaction vessel (B2) and / or the storage container (B1), if necessary, a crushing device (Z2) is connected upstream.

Device according to one of claims 20 to 22, characterized in that a metering device (Z1), in particular a speed-controlled conveyor screw, introducing material (E2) and / or that the circulation pump (P1) of the storage container (B1) mixes the entry material (E2) and / or heats up, the water content evaporates.

Device according to one of the preceding claims, characterized in that by throttling with the throttle (D2), the pressure (61) behind the pump (P2) is so high adjustable that behind the throttle (D2) cavitation occurs. 25. Device according to one of the preceding claims, characterized in that by throttling with the throttle (D2) the pressure (61) behind the pump (P2) is so high that behind the throttle (D2) cavitation occurs whose intensity over the pressure (61) is adjustable, thereby assisting the mixing and / or comminution and / or outgassing.

Device according to one of the preceding claims, characterized in that in the storage container (B1) and / or in the reaction vessel (B2) over the entire container height in each case an analog level measurement (L1, L2) is set up and / or that for both containers (B1, B2 ) technically relevant level levels are adjustable to serve as a control criterion.

27. Device according to one of the preceding claims, characterized in that in the storage tank (B1) and / or in the reaction vessel (B2) below the minimum level (L1 1, L21) in each case a redundant temperature measurement (T3, Τ3 ', T4, Τ4') is attached, in particular in order to act as an actual value for acting on the speed adjustment of the circulation pump temperature control.

28. Device according to one of the preceding claims, characterized in that for detecting cavitation of the circulation pump (P1) and / or the circulation pump (P2) each have an empirically determined curve (50, 51).

29. Device according to one of the preceding claims, characterized in that for detecting cavitation of the circulation pump (P1) and / or the circulation pump (P2) each have an empirically determined curve (50, 51), in which the electrical drive power of the pump ( P1, P2) is shown as a function of its rotational speed during normal operation in order to detect cavitation of the pump (P1, P2) in a different manner with a negative deviation from this.

30. Device according to one of the preceding claims, characterized in that for detecting cavitation of the circulation pump (P1) and / or the circulation pump (P2) each have an empirically determined curve (50, 51), in which the electrical drive power of the pump ( P1, P2) is shown as a function of its speed during normal operation in order to have available by a positive deviation, a signal and / or indicator for the accumulation of non-volatile solids available. 31 Device according to one of the preceding claims, characterized in that the throttle bodies (D1, D2) are designed as a single nozzle or single diaphragm or of several switchable nozzles or diaphragms.

Device according to one of the preceding claims, characterized in that subsequent to the throttle point (D2), in particular to the throttle point (D2) of the reaction vessel (B2), a straight pipe section (21) having a length greater than the length of a cavitation jet formed therein is available.

Apparatus according to claim 32, characterized in that the inner wall of the straight pipe section (21) has a sufficient lateral distance to the cavitation after the throttle point (D2), preferably to avoid damage to the pipe section by cavitation.

Device according to one of the preceding claims, characterized in that the system and / or device is equipped with a cogeneration unit CHKW, which is preferably operable with the fuel obtained from the system and / or at different locations (B3, B4, B5, B6 , K4, K5) in the system and / or device inevitably fig emerging and not further processed vapors sucks and burns.

35. Device according to one of the preceding claims, characterized in that the combined heat and power plant CHP is operated instead of a gas engine M with a gas turbine, which preferably emits heat energy at a higher temperature level.

36. Device according to one of the preceding claims, characterized in that storage containers (B3, B4) are present, which are preferably both heated with energy from the combined heat and power plant CHP,

37. Apparatus according to claim 36, characterized in that a storage container (B3) via the heat exchanger (W3) is maintained at a temperature below the boiling point of water and / or that the other reservoir (B4) via the heat exchanger (W4) below the reaction temperature of the current entry material (E1).

38. Device according to one of the preceding claims, characterized in that the temperature in the reaction vessel (B2), as long as no product is added, in addition to the energy input by the circulation pump (P2) and / or by the electric heater (EH2) and by the Heat exchanger (W2), which is integrated into the suction line (7) and / or is supplied with the high-temperature waste heat of the cogeneration unit CHP, is affected.

39. Device according to one of the preceding claims, characterized in that the volumetric pump (P3) a predetermined amount before the heat exchanger (W2), which was previously decoupled by closing a valve (V10) from the circulation in the suction line (7) Circulation pump (P2) feeds and / or that for circulating a strand (9) by opening a valve (V1 1) is connected in parallel to the heat exchanger (W2).

40. Device according to one of the preceding claims, characterized in that, as long as the volumetric pump (P3) promotes the outlet temperature (T9) of the heat exchanger (W2) as a function of the ak- tuellen temperature (T4, T4 ') in the reaction vessel (B2) by supplying heat energy via valve (V7) is regulated.

41. Device according to one of the preceding claims, characterized in that both catalyst and neutralizing agent, preferably in a known ratio mixed with carrier oil, each in a storage tank (B5, B6) are included.

42. Device according to one of the preceding claims, characterized in that both catalyst and neutralizing agent, preferably in a known ratio mixed with carrier oil, in each case in a storage tank (B5, B6) are mixed there with agitator (R1, R2) mixed and / or are permanently mixed and / or in each case with a variable-speed volumetric pump (P4, P5) in the suction line of the circulation pump (P2) can be entered, the pump (P4, P5) preferably in a dependent ratio to the speed of the pump (P3) controllable are.

43. Device according to one of the preceding claims, characterized in that a differential pressure measurement (76, 66) between pressure in the dome of the container (B1) and / or container (B2) and atmosphere is attached.

44. Device according to one of the preceding claims, characterized in that a differential pressure measurement (76, 66) between pressure in the dome of the container (B1) and / or container (B2) and atmosphere is attached, which is the actual value for a pressure regulator (78, 67), which controls the condensation (K1, K3) at the outlet of the container (B1, B2) and monitors for deviation in both the positive (69) and negative (68) directions, preferably by an alarm in the condensation (K1, K3) indicate and / or in the case of a large positive deviation the power supply by pump (P1) and / or pump (P2) and heat exchanger (W1) and / or heat exchanger (W2) to stop and / or the material flow via pumps (P1, Z1, Z2, P6) and / or pumps (P3, P4, P5).

Device according to one of the preceding claims, characterized in that a common container (90) for collecting both the condensed process water and the condensed middle distillate is used and / or that the level with two float level measurements (91, 92) is measured.

Apparatus according to claim 45, characterized in that the

Floats (93, 94) are designed for different density and / or that the level of the lighter middle distillate is mathematically corrected with the level of heavier process water.

47. A process for the catalytic and / or pressure-free treatment in a device, in particular according to one of the preceding claims, with an entry system for entry material, with a reaction vessel (B2), preferably a heat exchanger (W2) and with a speed-controlled

Circulation pump (P2), wherein the temperature (T4) in the reaction vessel (B2) is regulated by heat input,

characterized,

that the circulation pump (P2) is monitored for cavitation and

- That the flow behind the circulation pump (P2) through a throttle point (D2) is throttled and / or throttled and / or is passed through a crushing device.

Process according to Claim 47, characterized by a condensation device (K3) adjoining the reaction vessel (B2) and / or wherein subsequently to the reaction vessel (B2) a condensation device (K3) is arranged.

49. The method according to claim 47 or 48, characterized in that the temperature (T4) in the reaction vessel (B2) is regulated by heat input by means of a heat input device.

50. The method according to any one of claims 47 to 49, characterized in that the temperature (T4) in the reaction vessel (B2) optionally by heat input by means of electric heater (EH2) and / or heat exchanger (W2) and / or circulating pump (P2) is controlled

51. Method according to one of claims 47 to 50, characterized in that for detecting cavitation in the circulation pump (P2) in this a temperature measurement (T2) is installed.

52. The method according to any one of claims 47 to 51, characterized in that for detecting cavitation in the circulation pump (P2) in this a temperature measurement (T2) and in the line (8) a further temperature measurement (T6) are installed, which are monitored for difference (53).

53. The method according to any one of claims 47 to 52, characterized in that the temperature (T2) in the circulation pump (P2) to maximum (55) is monitored to automatically activate a shutdown of the power supply.

54. The method according to claim 52 or 53, characterized in that the

Temperature (T2), in particular the temperature (T2) in the circulation pump (P2), to maximum (55) is monitored in order to activate a pre-alarm and, with further increase automatically a shutdown of the energy supply. especially to reliably prevent the formation of toxic substances.

55. The method according to any one of claims 47 to 54, characterized in that the throttle point is adjustable and / or adjusted.

56. The method according to any one of claims 47 to 55, characterized in that the volume flow and / or pressure downstream of the circulation pump (P2) through the throttle point (D2) is throttled and / or adjusted so that behind the throttle point (D2) cavitation occurs , in particular to thereby assist the mixing and / or comminution and / or outgassing.

57. The method according to any one of claims 47 to 56, characterized in that the pressure (61) behind the circulation pump (P2) by adjusting the

Throttle (D2) is set.

58. The method according to any one of claims 47 to 57, characterized in that the pressure (61) behind the circulation pump (P2) by adjusting the throttle (D2) is set to the control range for energy input through the circulation pump (P2) in the direction of lower To expand energy.

59. The method according to any one of claims 47 to 58, characterized in that the inlet height (H2) to the speed-controlled circulating pump (P2) is selected so high that in the circulation pump (P2) over the entire

Speed range no cavitation occurs, and / or that the inlet height (H2) to the speed-regulated circulation pump (P2) is selected so high that at undisturbed suction conditions in the circulation pump (P2) over the entire speed range no cavitation occurs. Method according to one of claims 47 to 59, characterized in that the circulating pump (P2) is monitored for cavitation and / or is adapted to automatically activate in good time before exceeding a critical process temperature, a shutdown of the power supply, in particular by the To prevent the formation of toxic substances.