WO2003016435A2 - Unpressurized liquefaction of residues - Google Patents

Abstract

The invention relates to a method and a device for unpressurized liquefaction of residues containing hydrocarbons, which describe the oil formation process in a temperature range of 300 to 430° C with similar catalysts, wherein the additives ensure both the separation and the detoxification and stabilization of the resulting oils. The resulting product quality from plastics, waste oils, animal products and fats and other substances containing hydrocarbons is similar to that of fuels, herein the resulting products are highly pure and free from toxic agents.

Description

 Pressureless liquefaction of residues

The invention relates to a method and a device for the pressureless compacting or liquefaction of biological or mineral residues with a high hydrocarbon content. The product consists almost exclusively of hydrocarbons, which in this form are suitable for use in energy and drive technology. The remaining solids, which cannot be converted into the liquid phase, are processed into valuable materials by mechanical, electrical and thermal drying and separation.

The processes of combustion, gasification, compacting into fuel briquettes and the pyrolysis of residues are known. The disadvantage of this method is the low yield of electrical energy in small plants. A higher electrical efficiency is only possible by converting the hydrocarbon components into fuels for diesel engines with electricity generators almost completely. Small plants in particular prevent garbage tourism, which, in the case of problem goods such as animal flours, not only consumes fuel for transport, but also causes health processes.

Starting from pyrolysis, a process was therefore sought that almost completely converts the hydrocarbons of the residues into a hydrocarbon concentrate and almost completely frees the remaining residues from these hydrocarbons. Nature succeeded in this hundreds of millions of years ago through the process of oil formation. The formation of the oxygen atmosphere on Earth is largely due to this process.

The dead, organic matter was not transported back to the air by the oceans and burned there, but sank on the ground, mixed with the clay minerals from the primeval oceans. There the sediments, which formed a kind of oil shale, changed over hundreds of millions of years at temperatures of around 120 ° C on average and formed the liquid petroleum. Due to the liquid and thus mobile state of the oil, the oils squeezed out of the sediments and migrated into layers of sand with sufficient gap volume for the spokes from which they are extracted today.

The aim of the invention is therefore to emulate and modify this process so that it is applicable not only to the renewable residues such as oils and fats, but also to the conversion of plastics and chlorine-containing oils and wood components. The aim of the invention is therefore to provide a method and an additive for use in the To find processes that, similar to the clay minerals in the primeval oceans, find the processes of detoxification, splitting into thin hydrocarbons and the stabilization by rearrangement of the final valences formed during the splitting. The stabilization serves to prevent subsequent thickening of the oils that form.

Furthermore, the aim of the invention is to carry out this process in seconds instead of in the long historical periods and in a form which ensures high product quality despite all impurities and additives, such as foaming agents, of the residues.

The process should also be suitable for mineral hydrocarbon products, such as waste oils with the phosphate component as foaming agents, plastics with chlorine and fluorine-containing substances, such as PVC and Teflon, and for the waste greases and complex hydrocarbons, such as distillation residues.

The essential object of the present invention is therefore to demonstrate a method in which the residues are converted into a usable form in material form without combustion and gasification.

According to the invention, to achieve the object, these substances are introduced into an oil circuit with a surface-active additive and heated between 300 and 450 ° C. and converted to oils in the boiling range from 100 to 350 ° C. A further advantageous embodiment of the method is specified in the subclaims.

Surprisingly, the complete solution to this problem has been found by raising the temperature of oil formation from 120 ° C to an average of 390 ° C, thereby shortening the process to seconds. The type of clay mineral that enables all 3 functions of detoxification, cleavage and stabilization to be economical and regenerable is calcium aluminum silicate in the form of the A 504 from Tricat.

The system form for the above-mentioned solution is characterized in that the circuits side by side of the circulation tube evaporator, in the circuit with the containment vessel and the circulation evaporator connected downstream on the flue gas side of the distillation system with return pipes and on the residue side for the discharged residues, the pressing screw, residual oil evaporation and electrolysis for the inorganic residues containing phosphate are.

The complete process sequence is described in detail with direct reference to FIGS. 1 and 2. Figure 1 shows the inventive method. The actual splitting and stabilization of the hydrocarbon concentrates produced are carried out in a circulation evaporator 1. In a distillation evaporator 2 connected downstream on the flue gas side, the oils thus produced are again distilled to high-quality oils. The starting burner in the form of an oil burner 3, in which the oil produced is burned for the starting process, is used to reach the reaction temperature of 390 ° C. This takes place in a combustion chamber 4, which is heated in the operating state with the gas from the vacuum pumps 10. In the operating state, there is no operation from the burner 3, which only supplies the combustion air during operation.

The circulation evaporator 1 has a honeycomb ceramic layer 5 on both sides, which ensures that the combustion chamber burns stably and the heating of the evaporator tubes works optimally due to the increased radiation portion of the heat transfer. The hydrocarbon vaporized with the aid of the splitting action of the calcium-aluminum-silicate added collects in a safety steam container 6. This is designed to be large in order to prevent foams which may arise from foaming agents from entering the product. The non-evaporated parts collect at the bottom of the containment and from there back into the circulation evaporator, which creates a cycle.

The two evaporators, the circulation evaporator 1 and the distillation evaporator 2 are connected to a discharge 7 which disposes of the settled solids from the two evaporators 1 and 2. On the product side, the vaporized substances that condense in the distillation column are discharged via the two product containers .8 and 9. The container 8 is an intermediate product tank for the temporary storage of oils for maintaining the liquid level in the circulation evaporator and the container 9 is the product tank for the storage of the end product.

In the case of water-containing input materials, the intermediate product tank 8 is the actual product tank and the product tank 9 is used to extract the water content. The gaseous product from the product tank 9 and the safety container 6 is sucked off into the combustion chamber via the vacuum pumps 10.

The right-hand vacuum pump only switches on in the event that the temperature in the safety container at the suction point drops due to the formation of water vapor. This removes water vapor from the atmosphere in the containment. The solids discharge is carried out by a screw press 11 with a press cylinder 12. The conical tapered press cylinder 12 increases the solids concentration by squeezing oil.

The safety technology for the handling of such a system with combustible oil is ensured by a control technology and in the event of an accident via a pressurized water extinguishing tank 13 with the contents of the extinguishing water 14 and a compressed air 15 located above it. In the event of an accident, the extinguishing water quantity becomes below by extinguishing with the pressurized water 14 the system collected and thus the groundwater pollution prevented by a fire water retention basin 16.

A stirrer 17 is used to supplement the mobilization of the solid which is being introduced and is formed. Care must be taken to ensure that the amount of solid in the reactor does not become too large in order not to impede the circulation. In a special embodiment, the solid is conveyed via a discharge screw into a riser pipe which is connected to an entry into the safety container above the liquid level of the circulating liquid. Below this entry is a separating sieve, on which the solid drips and from which the solid is periodically discharged to the outside through an opening and scratches.

The advantage of such an additional separation of solid matter is the continuous discharge when the pipeline is fully open, which forms an additional, separating circuit to the safety container. This cycle ensures the permanent separation of solids that form and relieves the liquid cycle of these substances. The separation via the bottom drain, on the other hand, is only carried out periodically after the system has been shut down, since exact dosing is necessary to prevent the lower container from being overfilled with the contents of the reactor.

Another innovative separation of catalytically non-evaporable solids is activated in the circuit between the tube evaporator and the safety container in such a way that the mixture of product steam and non-evaporated liquid coming from the tube evaporator tangentially opens into a hydrocyclone 48 below the safety container, which flows upwards opens into the safety container and downwards into a liquid container 49, which is connected in the upper part to the lower part of the circulation evaporator and thereby ensures the circulation.

The solid matter discharged by the screw press 11 is conveyed into a discharge screw 18 after the pressing screw 12 and is further dried there by indirect heating. From there, the expelled oil vapor reaches the safety container. Also in the flue gas stream is an entry screw 19, in which the substances entered from an entry 20 are dried by indirect heating by the flue gas and are introduced directly into the circulating liquid through the subsequent entry pipeline. The entry into the liquid prevents the steam from being contaminated with small-grain entry goods, such as prion-contaminated animal meal, and thus ensures 100% conversion of the entered problem substances.

The flue gases cooled in this way pass through a flue gas pipe 21 to the outside. In the heating-up state, condensate arises that condenses in the flue gas pipe 21 and is discharged to the outside by a condensate drain with neutralization 22.

The flue gas is cooled to 450 ° C in the circulation evaporator stage, to 350 ° C in the distillation evaporator, to 250 ° C in the after-dryer and to 150 ° C in the input material dryer. For the start phase, the dryers are provided with additional burners, which ensure the necessary minimum temperature.

The product generation in the distillation evaporator 2 is supported by a foam brake 23, which ensures that only steam without the liquid portion of a foam reaches a distillation column 24 and the product is thus produced particularly cleanly.

In the distillation column 24, the low boilers are formed at the upper end of the column and are removed on a line 25. The product arises in the underlying floors and is taken from the lines 26. The distillation column is expediently a bubble tray column. ,

The product specification is given by the boiling temperature of the respective column section and the trays and thus ensures the control of the products. This is done by a condenser 27 and a solenoid valve 29. A backwash 30 is activated to lower the product evaporation temperature. At the end of the condenser 27, a vacuum line 28 is attached, which opens into the product container 9. The values to be set as the mean boiling point of the product hood are 270 ° C for diesel oil, 280 ° C heating oil, 250 ° C kerosene and 160 ° C for petrol in the case of high aromatics.

The condenser receives its cooling water through a cooling water inlet 31. In countercurrent, the cooling water passes through the condenser and then reaches a cooling water outlet 32.

If, despite the cooling and the vacuum pump, the pressure of the system rises above a set value, the excess gas enters the through a pressure relief valve 33 Torch. The pressurized water openings and the extinguishing water pressure nozzles 34 also serve to control critical operating states. There, the temperature of the hottest zone of the system is cooled from 390 ° C to the uncritical lower ignition temperature of below 320 ° C with a cooling water flow in the event of an accident or critical operating state.

The input substances which are introduced into the system at the entry 20 via a metering are the residual substances 35, a catalyst 36 and the lime 37. The catalyst is introduced in the form of a fine powder in order to be homogeneously suspended in the circulation evaporator. Sodium aluminum silicate is used instead of calcium magnesium silicate. The lime then converts this sodium aluminum silicate into calcium silicate by ion exchange. This makes the calcium-magnesium silicate the effective substance even when sodium magnesium silicate is input.

This conversion is always given in particular when using plastic waste, since the PVC contained in the plastic waste takes the sodium portion of the catalyst through salt exchange or replaces it with hydrogen by ion exchange. Through the subsequent reaction of the catalyst with the lime or hydrated lime, the catalyst will then always take the form of calcium magnesium silicate and act as an active substance. The lime is dosed via the pH measurement in the gas after the vacuum pump by switching the dosing on until the pH drops again until pH 7 is reached again. Soda or caustic soda can be used instead of lime.

For the preparation or cleaning in front of the vacuum pump of the product gases introduced into the burner, the still liquid components are released in a high-speed cyclone 38.

This consists of a cyclone, the inlet nozzle of which is extended in the form of a Venturi nozzle. As an extension to the inlet, the nozzle has a narrowing part in which the speed is increased to values of approx. 100 m / s, a parallel part with at least 5 times the diameter and an expanding part with a 6 ° extension from a 3 to 6 -fold diameter. The stabilized flow separates the liquids much better. The oil components pressed out at the discharge are pumped back into the safety container 6 by a heavy oil pump 39.

The oil pumped by the heavy oil pump 39 serves, like the oil from the intermediate product container 9, to maintain the liquid level in the circulation evaporator 1, the liquid circulation of which and therefore reliable operation depends on it, that the circulation of the oil between the circulation evaporator and the safety container is maintained with a sufficient liquid level.

Heavy oils are important in the cycle, since the reaction should take place with the substances entered and not with the circulating liquid. These should be largely preserved in order to maintain the liquid cycle. The system is therefore being started for the first time with a hard-to-evaporate water-poor oil, a type of thermal oil, as is used for heat exchangers with thermal oil. These oils are continually supplemented by the more difficult-to-split fractions of the feedstocks, such as the asphaltenes of the residual oils, which, however, are also split at elevated catalyst temperatures.

The solids deposited in the evaporators at the lower end of the evaporators are discharged via flaps or metering screws, the solenoid valves 40. The signals for this are given by the thermocouples 43 which, in the case of deposits at the lower end, bring about the lowering of the temperature compared to the evaporator contents as a signal for the discharge. So if solids settle, they ensure a temperature reduction on the thermocouple compared to the circulating liquid. If this temperature drop has exceeded a value, the discharge is activated until the value falls below again. This automates the periodic, continuous discharge.

The supply of the heavy oils from the intermediate product container 9, additional waste oil containers for waste oils and waste oils to be processed and the heavy oil pump 39 is provided by a float switch 41 in the safety container. If the required liquid level drops below a value, the oils are added until the level is reached again. The signal for the addition of the lime 36 is given by a pH sensor 42 in the vacuum line. The signals for the temperature controls are given by the temperature and measuring sensors 43. Not only are these used to control the flaps on the discharge, but the temperature sensors also serve as measuring sensors for the elements of the system's heat generation and the quantity of the added catalyst quantity.

The temperature sensor in the circulation evaporator above the tube bundle increases the amount of catalyst with increasing temperature, since the reaction is then increased and the temperature is lowered. When the temperature drops, the additional burner is started. After the reaction temperature has been reached and the vacuum pump has reached a sufficient speed, i.e. the required minimum speed for the gas supply has been reached, the start burner is switched off. If the temperature then drops, the vacuum is increased and only when the temperature drops further does the burner again ignited.

If the temperature continues to rise, the amount of entry that cools the system is increased. The temperature is controlled with the amount of the entry. In the event of a further increase, the amount of gas to the burner is reduced by metered opening of the gas flow to the torch. An energy supply can also result from the suction of the water vapor generated in the safety container.

The water vapor and low boiler components that occur when the temperature is wet at lower temperatures are discharged at the upper end of the safety container at a water separator 44 and are introduced into the combustion chamber in a dried state by the liquid components via the high-speed cyclone 38.

The vacuum pump connected to this circuit is separated by a solenoid valve during the non-operation phase in order not to endanger the vacuum. Both gas flows, from the condenser and from the water separator, reach the combustion chamber 4 via a gas line 45 and ensure thermally stable operation without the supply of external energy. The amount of gas in the total amount of product is approximately 3 to 7% in terms of energy. On average, 4.5% gas, based on the input material or the product, is generated.

The control ensures that the gas volume is always adapted to the energy requirements of the system. A safety line 46 to the torch is therefore only open in the event of a sudden overproduction. In order to make better use of this gas energy, the evaporator tubes in the rear part are equipped with ribs, coated with a metal sponge or with an improved flow with the flame deflection plates 47. These baffles increase the flue gas path and thus ensure better heat transfer to the evaporators.

Figure 2 shows the inventive device. A circulation evaporator 51 consists of a cylindrical container with a tube bundle. The tubes seen in the direction of the flames are not finned. The pipes lying to the rear in the radiation shadow of the pipes have ribs, surface-enlarging structures, such as foam metal casting or baffle plates. The circulation evaporator 51 has collecting chambers below and above the tubes, which are connected to an adjacent safety steam container 56 with tubes and thus form a circuit.

A hydrocyclone 98 is arranged below the safety steam container 56, which, with an underlying liquid container 99 and the connecting pipeline between the Circulation evaporator and this liquid container 99 forms a circuit. At the lower end of the liquid container 99, a pump for removing the solids is arranged.

To the right of the circulation evaporator 51 is a distillation evaporator 52 connected downstream on the flue gas side, via which the distillation column is arranged. To the left is the starting burner in the form of an oil burner 53, which is mounted on a ceramic-lined combustion chamber 54. The gas line, which is connected to the vacuum pumps 60, opens into this. The burner 53 has a separate circuit for the air and the oil supply, which is temporarily blocked during operation, while the combustion air fan is always switched on during operation.

The circulation evaporator 51 has a honeycomb ceramic layer on both sides, which is constructed from honeycomb ceramic blocks of 50 to 100 mm in thickness. The material is preferably magnesium aluminum silicate (cordierite). The safety steam container 56 is arranged above the oil burner 53.

This is large and has foam-reducing fittings. It has the connecting lines to the circulation evaporator 51 and forms a liquid circuit with it.

The two evaporators, the circulation evaporator 51 and the distillation evaporator 52 are connected to a discharge 57 which is arranged underneath. It is connected to the two evaporators 51 and 52. Above is the distillation column, which preferably consists of a bubble cap column. This has outlets on the floors, which are connected to pipes and drainage containers. These are the two product containers 58 and 59.

The container 58 is an intermediate product tank, preferably a cylindrical unpressurized container, which is approved for the storage of oils. It is connected to the safety steam tank by a line and a feed pump, which is switched via the level switch. The tank 59 is the product tank for storing the end product, i. H. the product containers are connected to different lines. The intermediate product container 58 is connected to the safety container via a pump. The product container 58 is connected to the consumer or a tank.

In the case of water-containing input materials, the intermediate product tank 58 is the actual product tank and the product tank 59 is used to extract the water content. The gaseous Product from the product tank 59 and the safety container 56 is sucked off into the combustion chamber via the vacuum pumps 60. The right-hand vacuum pump only switches on in the event that the temperature in the safety container at the suction point drops due to the formation of water vapor. This removes water vapor from the atmosphere in the containment.

The solids discharge is carried out by a screw press 61 with a press cylinder 62. The conically tapered press cylinder 62 increases the solids concentration by squeezing oil. The safety technology for the handling of such a system with combustible oil is ensured by a control technology and in the event of an accident via a pressurized water extinguishing tank 63 with the contents of the extinguishing water 64 and the compressed air 65 located above it. In the event of an accident, extinguishing with the pressurized water 64 causes the groundwater to become contaminated an extinguishing water retention basin 66 prevented.

A stirrer 67 is used to supplement the mobilization of the solid that is being formed and is formed. This is arranged on the circulation evaporator in such a way that the stirrer protrudes through one of the pipes to below the pipes and thus reaches the liquid below the pipes. The solid that is then discharged is conveyed into a discharge screw 68 after a pressing screw 62 and is further dried there by indirect heating. From there, the expelled oil vapor reaches the safety container.

An entry screw 69 is also located in the chimney or exhaust pipe arranged at the end. It has a double wall, in the intermediate wall the flue gas is guided separately from the contents of the screw. The screw has a connecting line to an entry 70. The flue gas line merges into a flue gas pipe 71. At the lower end of the flue gas pipe 71 there is a condensate drain with neutralization 72 with a condensate drain to the outside.

A foam brake 73 is arranged in the distillation evaporator 52. It consists of sieves or metallic sponge castings arranged one above the other and is located below a distillation column 74. In the distillation zone 74, the low boiler fraction is removed via a line 75. The product arises in the underlying floors and is removed from the lines 76 by connecting the raw line attached to the floor to the product container.

Temperature sensors are arranged above the bottoms of the distillation zone and are electronically connected to the liquid drain solenoid valves. The circuit opens the Solenoid valves within a defined temperature in which the quality of the product is given. The product specification is given by the boiling temperature of the respective column section and the trays and thus ensures the control of the products. This is done by a condenser 77 and a solenoid valve 79. A backwash 80 and the solenoid drain valve are electrically activated with the electrical connection line to the product temperature display. At the end of the condenser 77, a vacuum line 78 is attached, which opens into the product container 59.

The condenser receives its cooling water through a cooling water inlet 81. In countercurrent, the cooling water passes through the condenser and then passes into a cooling water outlet 82. If, despite the cooling and the vacuum pump, the pressure of the system rises above a set value, the excess gas passes through a pressure relief valve 83 in the torch.

The extinguishing water pressure nozzles 84 are also connected to solenoid valves which are electrically connected to flame and flue gas detectors and receive their opening impulse from there. With a cooling water flow in the event of an accident or critical operating state, the temperature of the hottest zone of the system is cooled from 390 ° C to the uncritical lower ignition temperature of below 320 ° C.

The input material input 70 is connected via a metering to the input of the residual materials 85, a catalyst 86 and the lime 87. The residual material contains hydrocarbons and has the form of animal meal, fat, waste oils, vacuum residue, plastics, wood meal or rubber. The catalyst is entered in the form of a fine powder and has the chemical structure of powdered calcium magnesium silicate or sodium aluminum silicate. This sodium-aluminum-silicate is then converted into calcium-magnesium-silicate by ion exchange. This makes the calcium-magnesium silicate the effective substance even when sodium magnesium silicate is input.

This conversion is always given, in particular when using plastic waste, since the PVC contained in the plastic waste removes the catalyst from the catalyst by ion exchange by salt formation or replaces it with hydrogen. Through the reaction of the catalyst with the lime or hydrated lime, the catalyst will then always take the form of calcium magnesium silicate and act as an active substance. The lime is dosed via the pH measurement in the gas after the vacuum pump by switching the dosing on until the pH drops again until pH 7 is reached again. Soda or caustic soda can be used instead of lime. The burner gas line is connected to a high-speed cyclone 88. This consists of a cyclone, the inlet nozzle of which is extended in the form of a Venturi nozzle. As an extension to the inlet, the nozzle has a narrowing part in which the speed is increased to values of approx. 100 m / s, a parallel part with at least 5 times the diameter and a widening part with a 6 ° widening and a 3 to 6 -fold diameter. The stabilized flow separates the liquids much better.

A heavy oil pump 89 is arranged in the discharge 57 and is connected to the safety container 56. A connecting line is also arranged between the intermediate product container 59 and the circulation evaporator 51. In the circulation evaporator 51 is a hard-to-evaporate water-poor oil, a kind of thermal oil, as it is used for the heat exchanger with thermal oil.

The solids deposited in the evaporators at the lower end of the evaporators are discharged via flaps or metering screws, the solenoid valves 90. These are electronically connected to the thermocouples 93 via a controller in the electronics and the frequency-converted motor of the flaps.

The heavy oil connection lines from the intermediate product container 59, residual oil container and the heavy oil pump 89 are given by a float switch 91 in the safety container. The signal for the addition of the lime 87 is given by a pH sensor 92 in the vacuum line. The signals for the temperature controls are given by the temperature and measuring sensors 93. In this way, they not only control the flaps on the discharge, but also the elements of the system's heat generation and the amount of catalyst added.

The temperature sensor in the circulation evaporator above the tube bundle is electrically connected to the metering device for the amount of catalyst. As the temperature rises, the metering device is regulated for greater addition.

When the temperature drops, the auxiliary burner is started. If it reaches the reaction temperature and the vacuum pump reaches the minimum speed required for the gas supply, it switches off. At then. falling temperature, the vacuum is increased and only when the temperature drops further, the burner is ignited again.

If the temperature continues to rise, the amount of entry that cools the system is increased. With the The amount of the entry is controlled by the temperature. In the event of a further increase, the amount of gas to the burner is reduced by metered opening of the gas flow to the torch. An energy supply can also result from the suction of the water vapor generated in the safety container. The water vapor and low boiler parts that occur when the temperature is wet at lower temperatures are discharged at the upper end of the safety container at a water separator 94 and are dried and introduced into the combustion chamber by the liquid parts via the high-speed cyclone 88.

The vacuum pump connected to this circuit is separated by a solenoid valve during the non-operation phase in order not to endanger the vacuum. Both gas flows, from the condenser and from the water separator, reach the combustion chamber 54 via a gas line 95 and ensure thermally stable operation without the supply of external energy. The amount of gas in the total amount of product is approximately 3 to 7% in terms of energy. On average, 4.5% gas is generated, based on the input material or the product.

The control ensures that the gas volume is always adapted to the energy requirements of the system. A safety line 96 to the torch is therefore only opened in the event of a sudden overproduction. In order to make better use of this gas energy, the evaporator tubes in the rear part are equipped with fins, coated with a metal sponge or, with an improved flow, with the flame deflection plates 97. The safety line 96 is equipped with a pressure relief valve for 0.2 to 0.5 bar pressure.

The safety line is connected outside the building with an overpressure pot, which is designed as a cyclone. At the bottom of this pot there is a liquid separator and condensate container. The gas discharge of the overpressure pot may be designed as a torch. To do this, an ignition device must be installed depending on the flow switch.

In one embodiment, the inventive method will be explained in more detail.

A circulation evaporator 1 has a volume of 500 liters and the distillation evaporator 2 located next to it also has 500 liters. The evaporator contains 100 tubes with a diameter of 2 inches and fins with a thickness of 2 cm. The first 3 rows of pipes facing the burner have no fins.

The start burner in the form of oil burner 3, with an output of 200 kW, is used to reach the reaction temperature of 390 ° C, in which the oil produced for the starting process is burned. This takes place in the combustion chamber 4 with a volume of 100 liters, which in the operating state is heated with the gas from the vacuum pumps 10 with a maximum output of 16 m ³ / h at 0.2 bar negative pressure. In the operating state, there is no operation from the burner 3, which only supplies the combustion air of 200 m ³ / h during operation.

The circulation evaporator 1 has a honeycomb ceramic layer 5 of 4 x 4 honeycombs 100 mm thick and 150 x 150 mm surface on both sides, which ensures that the combustion chamber burns stably and the heating of the evaporator tubes works optimally due to the increased radiation portion of the heat transfer. The hydrocarbon vaporized with the aid of the splitting action of the calcium-aluminum silicate added collects in the safety steam container 6 with a volume of 5 m ³ .

This is designed to be large so that foams that may arise from foaming agents do not get into the product. The non-evaporated parts collect at the bottom of the safety container and are separated in a hydrocyclone on the underside under the safety container and from there they get back into the circulation evaporator via a liquid and sludge separator container with a volume of 500 l and a connecting pipe with DN 200 forms a cycle.

The two evaporators, the circulation evaporator 1 and the distillation evaporator 2, are connected to the discharge 7 with a content of 0.5 m ³ , which disposes of the settled solids from the two evaporators 1 and 2. On the product side, the vaporized substances that condense in the distillation zone with a diameter of 0.4 m and a height of 6 m and are discharged via the two product containers 8 and 9 each with a content of 1 m ³ . The container 8 is an intermediate product tank for the temporary storage of oils for maintaining the liquid level in the circulation evaporator and the container 9 is the product tank for the storage of the end product.

In the case of water-containing input materials, the intermediate product tank 8 is the actual product tank and the product tank 9 is used to extract the water component. The gaseous product from the product tank 9 and the safety container 6 is sucked off into the combustion chamber via the vacuum pumps 10. The right-hand vacuum pump only switches on in the event that the temperature in the safety container at the suction point drops due to the formation of water vapor. This removes water vapor from the atmosphere in the containment.

The solids discharge is through the screw press 11 with the press cylinder 12 carried out. This has a diameter of 250 mm and a screw height of 80 to 50 mm tapering. The conically tapered press cylinder 12 increases the solids concentration by squeezing oil. Around the screw press is a perforated screen cylinder with holes of 1 mm in diameter. In the case of plastics with 3% PVC, the discharge amount is 6%, consisting of 3% calcium chloride, 1% catalyst in the form of calcium aluminum silicate and 2% residual oil. With an input of 550 kg / h plastic, the product quantity is 500 kg / h oils in the boiling range of the heating oil EL.

The safety technology for the handling of such a system with combustible oil is guaranteed by a control technology and in the event of an accident via the pressurized water extinguishing container 13 with a total content of 10 m ³ with the contents of the extinguishing water 14 and the compressed air 15 above With the extinguishing water 14, the amount of extinguishing water is collected below the system, thus preventing the groundwater from being contaminated by the extinguishing water retention basin 16 with a total volume of 20 m ³ .

The agitator 17 is used to supplement the mobilization of the solid that is being formed and is formed. The solid that is then discharged is conveyed into the discharge screw 18 after the pressing screw 12 and is further dried there by indirect heating. It also has a diameter of 250 mm and a length of 1 meter. It is double-walled with a flue gas space of 40 mm. From there, the expelled oil vapor reaches the safety container.

Also in the flue gas stream is the feed screw 19, also 25 mm in diameter, 1 m in length and a flue gas space of 40 mm, in which the substances entered from the feed 20 are dried by indirect heating by the flue gas and are fed directly into the circulating liquid through the subsequent feed pipe become. The entry into the liquid prevents the steam from being contaminated with small-grain entry goods, such as prion-contaminated animal meal, and thus ensures 100% conversion of the entered problem substances.

The flue gases cooled in this way reach the outside through the flue gas pipe 21 with a diameter of 250 mm. In the heating-up state, condensate arises that condenses in the flue gas pipe 21 and is discharged to the outside by the condensate drain with neutralization 22. The flue gas is cooled to 450 ° C in the circulation evaporator stage, to 350 ° C in the distillation evaporator to 250 ° C in the after-dryer and to 150 ° C in the input material dryer. For the start phase, the dryers are provided with additional burners, which ensure the necessary minimum temperature. The product generation in the distillation evaporator 2 is supported by the foam brake 23, which ensures that only steam without the liquid portion of a foam gets into the distillation zone 24 and the product is thus produced particularly cleanly. The foam brake has a sponge cast structure made of aluminum and a thickness of 4 mm. In the distillation zone 24 with 20 trays in 5 shots of 4 trays and 30 mm from the bottom, the low boilers are formed at the upper end of the column and are removed from line 25. The product arises in the underlying floors and is taken from the lines 26. The distillation column is a bubble tray column.

The product specification is given by the boiling temperature of the respective column section and the trays and thus ensures the control of the products. This is done by the condenser 27 and the solenoid valve 29. The backwash 30 is activated to lower the product evaporation temperature.

At the end of the condenser 27, the vacuum line 28 is attached, which opens into the product container 9. The values to be set as the average boiling point of the product fume cupboard are 270 ° C for diesel oil, since the raw material is plastic with predominantly PE and PP.

The condenser has a cooling capacity with water of up to 200 kW. He receives his cooling water through the cooling water inlet 31 with a diameter of 1.5 inches. In countercurrent, the cooling water passes through the condenser and then reaches the cooling water outlet 32. If, despite the cooling and the vacuum pump, the pressure of the system rises above a set value, the excess gas reaches the torch via a pressure relief valve 33.

To control critical operating conditions, the pressurized water openings for a water flow rate of 100 l / min are also used for 1 and 2 minutes through the extinguishing water pressure nozzles 34. There, the temperature of the hottest zone of the system is raised to 390 ° C in the event of an accident or critical operating state the uncritical lower ignition temperature has cooled down to below 320 ° C.

The input materials which are introduced into the system at entry 20 via a metering are the residual materials 35, the catalyst 36 and the lime 37. The catalyst is introduced in the form of a fine powder in order to. to be present homogeneously suspended in the circulation evaporator. 6 kg / h calcium aluminum silicate are used. 15 kg of lime are added per hour controlled by the pH probe. This means that even if you enter sodium magnesium silicate calcium-magnesium-silicate is the effective substance.

For the preparation or cleaning in front of the vacuum pump of the product gases introduced into the burner, the still liquid components are released in a high-speed cyclone 38. This consists of a cyclone, the inlet nozzle of which is extended in the form of a Venturi nozzle. As an extension to the inlet, the nozzle has a narrowing part in which the speed is increased to values of approx. 100 m / s, a parallel part with at least 5 times the diameter and an expanding part with a 6 ° extension and a 3 to 6 -fold diameter. The stabilized flow separates the liquids much better. The cyclone has a diameter of 300 mm and a narrowest diameter in the venturi inlet of 15 x 25 mm.

The oil components pressed out at the discharge are pumped back into the safety container 6 by the heavy oil pump 39 with a pumping capacity of 50 l / h. They serve, like the oil from the intermediate product container 9, to maintain the liquid level in the circulation evaporator 1, the liquid circulation of which and therefore reliable operation depends on the circulation of the oil between the circulation evaporator and the safety container being maintained with a sufficient liquid level.

Heavy oils are important in the cycle, since the reaction should take place with the substances entered and not with the circulating liquid. These should be largely preserved in order to maintain the liquid cycle. The system is therefore being started for the first time with a hard-to-evaporate water-poor oil, a type of thermal oil, as is used for heat exchangers with thermal oil. These oils are continually supplemented by the more difficult-to-split fractions of the feedstocks, such as the asphaltenes of the residual oils, which, however, are also split at elevated catalyst temperatures.

The solids deposited in the evaporators are discharged at the lower end of the evaporators via flaps or metering screws with a diameter of 25 mm, the solenoid valves 40. The signals for this are given by the thermocouples 43 which, in the case of deposits at the lower end, bring about the lowering of the temperature compared to the evaporator contents as a signal for the discharge.

So if solids settle, they ensure a temperature reduction on the thermocouple compared to the circulating liquid. If this temperature drop has exceeded a value, the discharge is activated until the value falls below it again. This automates the periodic, continuous discharge. The supply of the heavy oils from the intermediate product container 9, additional waste oil containers for waste oils and waste oils to be processed and the heavy oil pump 39 is given by the float switch 41 in the safety container. If the required liquid level drops below a value, the oils are added until the level is reached again. The signal for the addition of lime 36 is given by the pH sensor 42 in the vacuum line. The signals for the temperature controls are given by the temperature and measuring sensors 43. Not only are these used to control the flaps on the discharge, but the temperature sensors also serve as measuring sensors for the elements of the system's heat generation and the quantity of the added catalyst quantity.

The temperature sensor in the circulation evaporator above the tube bundle increases the amount of catalyst with increasing temperature, since the reaction is then increased and the temperature is lowered. When the temperature drops, the auxiliary burner is started. After reaching the reaction temperature and at a sufficient speed of the vacuum pump, d. H. the required minimum speed of the vacuum pump for the gas supply is reached, the start burner is switched off. When the temperature drops, the vacuum is increased and only when the temperature drops further, the burner is ignited again. The limit temperature for the self-sufficiency of the reaction with the gas is 410 ° C with this feed.

If the temperature rises further, the amount of entry that cools the system is increased, the temperature in the containment then being about 100 ° C. lower than in the circulation evaporator. The temperature is controlled with the amount of the entry. In the event of a further increase, the amount of gas to the burner is reduced by metered opening of the gas flow to the torch. An energy supply can also result from the suction of the water vapor generated in the safety container. The water vapor and low boiler parts which occur when the entry is wet at lower temperatures are discharged at the upper end of the safety container at the water separator 44 and, after being dried, are introduced into the combustion chamber via the high-speed cyclone 38.

The vacuum pump connected to this circuit is separated by a solenoid valve during the non-operation phase in order not to endanger the vacuum. Both gas flows, from the condenser and from the water separator, reach the combustion chamber 4 via the gas line 45 and ensure thermally stable operation without the supply of external energy. The amount of gas generated in the total amount of product is 4.5% gas, based on the input material or the product. The control ensures that the gas volume is always adapted to the energy requirements of the system. The safety line 46 to the torch is therefore only opened in the event of a sudden overproduction. To make better use of this gas energy, the evaporator tubes are coated with metal sponge in the rear part and the flow is improved with the flame deflection plates 47. These baffles increase the flue gas path and thus ensure better heat transfer to the evaporators.

In a further exemplary embodiment, the inventive device is described in more detail. The circulation evaporator 51 consists of a cylindrical container with a tube bundle of 100 tubes with a diameter of 2 inches and a height of 1200 mm. The collecting chambers at the lower and upper ends have a height of 300 mm. The tubes seen in the direction of the flames are not finned. The pipes lying to the rear in the radiation shadow of the pipes have ribs, surface-enlarging structures, such as cast metal foam or deflection plates. The circulation evaporator 51 has collection chambers below and above the pipes, which are connected to the adjacent safety steam container 56 with pipes and thus form a circuit.

The hydrocyclone with a tangential inflow pipe opening of DN 150 is located below the safety steam container and at the lower end of the safety steam container is a liquid container with a diameter of 600 mm and a height of 1 m. In the upper part there is a connection line from DN 250 to the circulation evaporator.

To the right of the circulation evaporator is the distillation evaporator 52 connected downstream on the flue gas side, via which the distillation zone is arranged. To the left is the starting burner in the form of the Herrmann oil burner 53 with a power of 200 kW, which is mounted on a ceramic-lined combustion chamber 54 with a diameter of 500 mm and a length of 800 mm. The gas line with a 2.5 inch diameter and a vacuum pump 60 with 16 m ³ / h gas suction capacity at 0.2 bar negative pressure opens into this.

The burner 53 has a separate circuit for the air of 200 m ³ / h and the oil supply of 20 l / h, which is temporarily blocked during operation, while the combustion air fan is always switched on during operation.

The circulation evaporator 51 has a honeycomb ceramic layer on both sides, which is constructed from honeycomb ceramic blocks of 50 to 100 mm in thickness. The honeycombs are 4 x 4 honeycombs with a cross-sectional area of 150 x 150 mm. The material is preferably magnesium Aluminum silicate (cordierite). A safety steam container 56 with a diameter of 2 m and a height of 3 m is arranged above the burner 53. This is large and has foam-reducing fittings. It has the connecting lines to the circulation evaporator 51 and forms a liquid circuit with it.

The two evaporators, the circulation evaporator 51 and the distillation evaporator 52, both of which are of identical design, are connected to the discharge 57, which is arranged underneath. It is connected to the two evaporators 51 and 52. Above is the distillation column, which consists of a bubble-cap column with a diameter of 400 mm, the base distance of 300 mm and 6 x 5 shots, ie. H. 6 floors are processed per shot. This has outlets on the floors, which are connected to pipes and drainage containers. These are the two product containers 58 and 59, each with a diameter of 1500 mm and a height of 2 m.

The container 58 is an intermediate product tank, preferably a cylindrical unpressurized container, which is approved for the storage of oils. It is connected to the safety steam tank by a line and a feed pump with a capacity of 1000 l / h, which is switched via the level switch. The container 59 is the product tank for storing the final product, i. H. the product containers are connected to different lines. The intermediate product container 58 is connected to the safety container via a pump at 500 l / h. The product container 58 is connected to the consumer or a tank.

In the case of water-containing input materials, the intermediate product tank 58 is the actual product tank and the product tank 59 is used to extract the water content. The gaseous product from the product tank 59 and the safety container 56 is sucked off into the combustion chamber via the vacuum pumps 60.

The right-hand vacuum pump only switches on in the event that the temperature in the safety container at the suction point drops due to the formation of water vapor. This removes water vapor from the atmosphere in the containment.

The solids discharge is carried out by the screw press 61 with a diameter of 250 mm with the press cylinder 62. The conically tapered press cylinder 62 increases the solids concentration by squeezing oil. The safety technology for handling such a system with combustible oil is guaranteed by a control technology and in the event of an accident via the pressurized water extinguishing container 63 with the content of 10 m ^{3 of} the extinguishing water 64 and the compressed air 65 above it. In the event of an accident, extinguishing with the extinguishing water 64 groundwater pollution from the fire water retention basin 66 with 20 m ³ prevented.

The agitator 67 serves to supplement the mobilization of the solid which is being formed and is formed. This is arranged on the circulation evaporator in such a way that the agitator projects through one of the tubes to below the tubes and thus reaches the liquid below the tubes. The solid that is then discharged is conveyed into the discharge screw 68 after the extrusion screw 62 and is further dried there by indirect heating. From there, the expelled oil vapor reaches the safety container.

Also in the chimney or exhaust pipe with a diameter of 250 mm arranged at the end is the feed screw 69 with a diameter of 250 mm. It has a double wall with a 50 mm cavity. The flue gas is guided in the partition wall separately from the screw content. The screw has a connecting line to the entry 70. The flue gas line merges into the flue gas pipe 71. At the lower end of the flue gas pipe 71 is the condensate drain with neutralization 72 with a condensate drain to the outside.

The foam brake 73 is arranged in the distillation evaporator 52. It consists of 6 sieves arranged one above the other and is located below the distillation zone 74. In the distillation zone 74, the low boiler fraction is removed via line 75 with a 1 inch diameter. The product arises in the underlying floors and is removed from the lines 76 by connecting the raw line attached to the floor to the product container.

Temperature sensors are arranged above the bottoms of the distillation zone and are electronically connected to the liquid drain solenoid valves with a diameter of 1 inch. The circuit opens the solenoid valves within a defined temperature, in which the quality of the product is given. The product specification is given by the boiling temperature of the respective column section and the trays and thus ensures the control of the products.

This is done by the condenser 77 and the solenoid valve 79 in a 1.5 inch line with a 1.5 inch solenoid valve. The backwash 80 and the magnetic drain valve are electrically activated with the electrical connection line to the product temperature display. At the end of the condenser 77, the vacuum line 78 is attached, which opens into the product container 59.

The condenser with 20 cooling water pipes with 1 inch diameter and a cooling capacity of Its cooling water receives 200 kW through the cooling water inlet 81. In countercurrent, the cooling water passes through the condenser and then passes into the cooling water outlet 82. If, despite the cooling and the vacuum pump, the pressure of the system rises above a set value, the excess gas passes through a pressure relief valve 83 in the torch. The extinguishing water pressure nozzles 84 are also connected to solenoid valves which are electrically connected to flame and flue gas detectors and receive their opening impulse from there.

With a cooling water flow in the event of an accident or critical operating state, the temperature of the hottest zone of the system is cooled from 390 ° C to the uncritical lower ignition temperature of below 320 ° C.

The input material input 70 with a capacity of 600 kg / h plastic is connected via a metering with the input of the residual materials 85, the catalyst 86 with 6 kg / h and the lime 87 with 15 kg / h. The residue contains hydrocarbons and is in the form of plastics. The catalyst is entered in the form of a fine powder and has the chemical structure of powdered calcium magnesium silicate.

This conversion is always given, especially when using plastic waste, since the PVC contained in the plastic waste removes the catalyst by ion exchange, the sodium by salt formation or replaces it with hydrogen. Through the reaction of the catalyst with the lime or hydrated lime, the catalyst will then always take the form of calcium-magnesium-silicate and act as an active substance. The lime is dosed via the pH measurement in the gas after the vacuum pump by switching the dosing on until the pH drops again until pH 7 is reached again. Soda or caustic soda can be used instead of lime.

The burner gas line is connected to a high-speed cyclone 88. This consists of a cyclone with a diameter of 300 mm, the inlet nozzle of which is extended in the form of a Venturi nozzle. As an extension to the inlet, the nozzle has a constricting part at a height of 15 x 25 mm, a parallel part with a length of 75 mm and an expanding part with a 6 ° extension of 60 mm length. The stabilized flow separates the liquids much better.

The heavy oil pump 89 with a delivery capacity of 100 l / h, which is connected to the safety container 56, is arranged in the discharge 57. A connecting line is also arranged between the intermediate product container 59 and the circulation evaporator 51. In the circulation evaporator 51 is a hard-to-evaporate water-poor oil, a kind of thermal oil, as it is used for the heat exchanger with thermal oil.

The solids deposited in the evaporators are discharged at the lower end of the evaporators via flaps or metering screws with a diameter of 250 mm, the solenoid valves 90. These are electronically connected to the thermocouples 93 via a controller in the electronics and the frequency-converted motor of the flaps.

The heavy oil connection lines from the intermediate product container 58, residual oil container and the heavy oil pump 89 are given by the float switch 91 in the safety container. The pH sensor 92 in the vacuum line gives the signal for the addition of the lime 87.

The signals for the temperature controls are given by the temperature and measuring sensors 93. In this way, they not only control the flaps on the discharge, but also the elements of the system's heat generation and the amount of catalyst added.

The temperature sensor in the circulation evaporator above the tube bundle is electrically interconnected with the metering device for the amount of catalyst. As the temperature rises, the dosing device is regulated for larger additions. When the temperature drops, the auxiliary burner is started. If it reaches the reaction temperature and the vacuum pump reaches the minimum speed required for the gas supply, it switches off. When the temperature drops, the vacuum is increased and only when the temperature drops further, the burner is ignited again.

If the temperature continues to rise, the amount of entry that cools the system is increased. The temperature is controlled with the amount of the entry. In the event of a further increase, the amount of gas to the burner is reduced by metered opening of the gas flow to the torch. An energy supply can also result from the suction of the water vapor generated in the safety container. The water vapor and low boiler parts that occur when the temperature is wet at lower temperatures are discharged at the upper end of the safety container at the water separator 94 and, after being dried, are introduced into the combustion chamber by the high-speed cyclone 88 via the high-speed cyclone.

The vacuum pump connected to this circuit is separated by a solenoid valve during the non-operation phase in order not to endanger the vacuum. Both gas flows, from the condenser and from the water separator, enter the gas line 95 through the Combustion chamber 54 and ensure a thermally stable operation without the supply of external energy. The amount of gas in the total amount of product is approximately 3 to 7% in terms of energy. On average, 4.5% gas is generated, based on the input material or the product.

The control ensures that the gas volume is always adapted to the energy requirements of the system. The safety line 96 to the torch is therefore only opened in the event of a sudden overproduction. In order to make better use of this gas energy, the evaporator tubes in the rear part are equipped with fins, coated with a metal sponge or, with an improved flow, with the flame deflection plates 97. The safety line 96 is equipped with an overpressure valve for 0.2 to 0.5 bar overpressure.

LIST OF REFERENCE NUMBERS

1 circulation evaporator 2 distillation evaporator

3 oil burners

4 combustion chamber

5 catalysts

6 safety steam tanks

7 discharge

8 Product container / intermediate product tank

9 Product container / product tank

10 vacuum pump

11 screw press

12 press cylinder / extrusion screw

13 pressurized water extinguishing tank

14 extinguishing water

15 compressed air

16 water retention tanks

17 agitator

18 discharge screw

19 feed screw

20 entry

21 Exhaust pipe / flue gas pipe

22 condensate drain m. Neutralization

23 foam brake

24 distillation units

25 line

26 line

27 capacitor

28 vacuum line

29 solenoid valve

30 backwash

31 Cooling water inlet

32 Cooling water drain / cooling water return

33 Safety valve / pressure relief valve

34 water pressure nozzles

35 residues catalyst

lime

High-speed cyclone

Heavy oil pump

magnetic valve

Float switch pH sensor.

Temperature and Sensor / thermocouple

water

gas pipe

safety line

Flame Deflector

cyclone unit

Absetzbehälter

oil pump

circulation evaporator

distillation evaporator

oil burner

combustion chamber

catalysts

Safety steam container

discharge

Product container / intermediate tank

Product container / product tank

vacuum pump

screw Press

Press cylinder / extruder screw

Pressure water extinguishing tank

fire water

compressed air

Fire water retention basins

agitator

discharge screw

feed screw

entry

Exhaust pipe / flue gas pipe

Condensate drain m. Neutralization 73 foam brake

74 distillation column

75 line

76 line

77 capacitor

78 vacuum line

79 solenoid valve

80 backwash

81 Cooling water inlet

82 Cooling water drain / cooling water return

83 Safety valve / pressure relief valve

84 Water pressure nozzle

85 residue

86 catalyst

87 lime

88 high speed cyclone

89 Heavy oil pump

90 solenoid valve

91 float switch

92 pH sensors

93 temperature and Sensor / thermocouple

94 water separator

95 gas pipe

96 Security line

97 flame deflector

98 cyclone unit / hydrocyclone

99 settling tanks / liquid tanks

100 oil pump

Claims

 claims 1. Process for the pressureless liquefaction of residues with a high hydrocarbon content, characterized, that these substances are added to an oil circuit with a surface-active additive between 300 and 450 ° C and converted to oils in the boiling range of 100 to 350 ° C. 2. The method according to claim 1, characterized, that the surface-active additive is an earth mineral in the active substance of calcium Aluminum silicate or by adding Kaik to the circulating oil is converted into this substance. 3. The method according to claim 1 and 2, characterized, that the input consists of the 3 components of hydrocarbon-containing residues, clay minerals in the form of calcium-aluminum-silicate or sodium that can be converted into this form Aluminum silicate and the lime is made. Method according to claim 3, characterized, that the supply takes place via a pipe directly into the circulating liquid or circulating oil, in which the supply pipe ends on or in the liquid. Method according to claim 1, characterized, that the system is kept under slight negative pressure by a vacuum pump so that the pressure at the inlet is close to atmospheric pressure. 6. The method according to claims 1 to 5, characterized, that the temperature of the circuit takes place through the resulting cracked gases by raising the additional burner and increasing the vacuum and lowering by supplying the substance and excess gas outlet. 7. The method according to claims 1 to 6, characterized, that a hydrozclone and a separating tank are attached below the safety tank, which close the circuit to the circulation evaporator and continuously separate the solids. 8. The method according to claims 1 to 6, characterized, that the formation of pollutants in the products chlorine and fluorine is prevented by the ion exchange action of the additive and other regeneration substances, such as lime or soda. Process according to claims 1 to 7, characterized, that the cleavage and stabilization reaction takes place in an oil circuit in which the catalyst is suspended and the circuit takes place with the heating from the cracking gas and cooling by the substances entered. Claim 10 10. Apparatus for carrying out the process of pressureless liquefaction of residues containing hydrocarbons, characterized, that a container system consisting of a circuit for carrying out the splitting, detoxification and stabilization of the oils in a tube bundle evaporator and a compensation and safety container for returning the liquid components is coupled to a combustion chamber for the combustion of cracked gas. 11. The device according to claim 10, characterized, that, in addition to the split part of the plant on the side remote from the burner, there is a flue gas-heated distillation plant which is connected on the product side to the steam space of the splitting plant. 12. The apparatus of claim 10 and 11, characterized, that the distillation plant is followed by a flue gas pipe with heating devices for the residual materials and the input materials. 3. Device according to claims 10 to 12, characterized, that the solids discharge after drying and heating is followed by an electrolysis, which the insoluble calcium phosphate residues from the processing of animal residues are converted into soluble monocalcium phosphates or phosphoric acid. 14. The apparatus according to claim 10, characterized, that the solids discharge from the lower part of the evaporator takes place via a conveyor, such as a screw conveyor, in a riser pipe, which leads above the liquid level of the system into one of the components, which has a separating screen below the inlet opening. 15. Device according to claims 10-14, characterized, that a hydrocyclone and a liquid container are arranged below the safety container, which are connected to the circulation evaporator 51 via pipeline.