CH703609A2 - Treatment of highly-loaded organic substance involves adding raw material mixture to reactor, cracking mixture in vacuum, drying, adding residual substances, and then condensing gaseous phase to liquid fuel - Google Patents

Abstract

Treatment of organic highly-loaded substance involves adding raw material mixture to a reactor, cracking mixture in vacuum, drying, adding residual substances, and then condensing the gaseous phase to liquid fuel.

Description

The invention relates to a method in which in the one and the same device, the treatment of lignocellulosic biomass to wood oil or mixed plastics and organic liquids based on petroleum to fuels, as well as mechanically prepared and predried household waste is processed into fuel gases and liquid fuels ,

With the pyrolysis method presented here, in one and the same reactor system in separate streams of lignocellulosic biomass, mixed plastics, and petroleum-containing sludges and sands can be melted by heating at hot contact surfaces under oxygen exclusion and the organic components are evaporated. This is in contrast to the so-called hot pyrolysis or gasification, in which by selective oxygen input takes place a semi-combustion and gases in the form of combustible oxide (CO) are obtained as synthesis gas.

The superheated steam is discharged from the reactor under vacuum and is then condensed and discharged at the lignocellulosic biomass as a pyrolysis oil and fuel gases, and coke.

In the treatment of mixed plastics and petroleum-containing sludges, the length of the hydrocarbon molecules in the pyrolysis gas is selectively determined before condensing in a partial condenser.

The long-chain and non-cracked hydrocarbon molecules are returned to the reactor to undergo the cracking process again. As a product in the pyrolysis of plastics, also called olefins or alkanes, and the oil-containing sludges is obtained as a base product fuel oil or naphtha, and fuel gases and slags are discharged in a dry form.

As a product in the pyrolysis of lignin and cellulose-containing materials wood oil, fuel gases and coke is obtained. The fuel gases and coke are used to generate the process energy and the wood oil can be used as fuel for stationary diesel engines to generate electrical energy.

Since there are a variety of organic compounds in the wood oil, the wood oil is advantageously used for the production of products in organic chemistry and pharmaceutical industry.

In the pyrolysis of the total household waste or fractions thereof, it must be previously mechanically processed and metals are separated. Before crushing is removed from the garbage, coarse and impurities and then advantageously pre-dried in a high-performance rotting with self-generated bioenergy. The fraction of household waste can also be introduced as wet mass in the reactors. In this case, about 10% of the product oil produced must be used to generate evaporative energy for dehydration.

From the Plastikanteil of household waste liquid fuels or naphtha are recovered and from the remaining organic, pyrolysis, which serves as a fuel for the production of methanol.

Naphtha or industrial gasoline is a refinery product from which plastic products are made based on the carbon atoms C1 to C12. C6 to C12 will be liquid at a temperature of less than 40 ° C, but the gaseous non-condensable C1 to C5 components can only be liquefied by cold treatment at temperatures below -65 ° C.

In order to avoid the aparativen and energetic effort, a plant for the production of so-called "vigin products" from waste plastics in the immediate vicinity of a refinery should be created so that synergy effects in the form of transport and energy, can be used optimally.

Fig. 1 shows the reactor (3) and the condensation plant (7) concerning the application for the material entry (1) of wood chips and other lignocellulosic biomass (3.14) for the production of wood oil (3.14.1), as well as recycled household waste (3.16) for the production of fuels (7.6), coke (5.15) and residues (5, 9, 1).

In addition to the functional description of Fig. 1, the Fig. 3und 7th

The material entry (1) and the entry of additives in the form of Schleissmaterial (1.1) and catalysts (1.2) in the reactor (3) takes place in cycles via the lock (2). Thus, no atmospheric oxygen is registered, the two gate valve (2.1) are mutually locked. Shown here is a lock (2). To ensure a continuous filling, several locks (2⋅n) can be arranged side by side.

After the completion of the lock (2), the contents with inert gas (2.2) is rinsed to displace the oxygen. After flushing the upper slide (2.1) is closed and then opened the lower slide (2.1). The lock contents fall into the feed chute (3.1) and are evenly distributed over the entire reactor width by the material distributor (3.2).

The drive (3.3) moves the auger (3.6) constantly by changing the direction of rotation (3.4) A and B, thereby distributes the registered fresh material (3.16.1) through the material distribution (3.5) alternately in the direction of A and B.

Via the drives (4.1), the material introduced is conveyed in the main flow direction (3.13) with the conveying spirals (4) The inner tube (6) is heated by the heating medium (6.3), which is enclosed by the heating jacket (6.1) and by Heating medium inlet (6.4) to the opposite heating medium outlet (6.5) flows.

By the contact of the biomass (3.14), as well as the treated household waste (3.16) with the hot surface of the inner tube (6), the biomass (3.14) and household waste (3.16) under oxygen occlusion and vacuum (7.2.1) melted at the hot contact surface. The resulting liquid film evaporates immediately and leaves as superheated steam (7.1), with a temperature between 380 to 420 ° C, via the gas dome (3.12) the reactor (3) and is via the gas line (7.1.1) of the condensation plant (7). fed.

The biomass (3.14) or the processed household waste (3.16) is melted directly at the hot contact surface of the inner tube (6). Due to the changing conveying direction (4.3) of the conveyor spiral (4), the biomass (3.14) or the treated household waste (3.16) is constantly mixed. In order to constantly obtain a thorough mixing, the rotation and conveying direction (A / B) is cyclically changed over a freely programmable stepping control.

In the rotation and conveying direction (B), the biomass (3.14) or the treated household waste (3.16) is conveyed back opposite to the main flow direction (3.13). In the rotation and conveying direction (A), the biomass (3.14) or the treated domestic waste (3.16) is conveyed in the main flow direction (3.13). In order to ensure the material throughput, the delivery spiral (4) must always convey at least one revolution more in the main flow direction (3.13) than is conveyed back in the opposite direction.

By reclaiming in the direction (B), the biomass (3.14) or the treated household waste (3.16) is compressed and pressed against the hot wall of the inner tube (6) and thereby the Abschmelzvorgang is accelerated.

In the material entry (1) of biomass (3.14) is added to clean the surface of the inner tube (6) of caking in the form of slag (4.6), a cleaning aid in the form of Schleissmaterial (1.1).

The required amount and composition of the wear material (1.1) depends on the composition and toughness of the material bed (3.19) and is advantageously made of broken waste glass and / or quartz sands.

It can also be pebbles or steel balls in the material entry (1), as Umlaufgut (1.4) and Schleissmaterial (1.1) are added, which after passing through the slag zone (3.9) and drying zone (12.7) in a sieve and not shown here Separator (1.3) at the output of the reactor (3) from the residue discharge (5.9) are separated and registered as Umlaufgut (1.4) again on the material entry (1).

By the lumpiness of the biomass (3.14) or the treated household waste (3.16), the vacuum (7.2.1) acts on the cavities in the bed and pulls the superheated steam (7.1) continuously from the reactor (3).

The superheated steam (7.1) with a temperature between 380 ° to 420 ° C, is sucked by the liquid jet pump (7.2), which at the same time generates the vacuum (7.2.1) in the reactor (3). The cooled propellant (7.11) consists of the product oil (7.6), which from the circulation container (7.5) with the circulation pump (7.7) of the liquid jet pump (7.2), or Venturi mentioned, is supplied. The superheated steam (7.1) mixes with the propellant (7.3) and is suddenly cooled, condensed and leaves as a mixture (7.4) of condensate, propellant and non-condensable gases, at a temperature of about 30 ° C, the liquid jet pump (7.2) and is relaxed in the circulation tank (7.5).

By the sudden cooling of the superheated steam (7.1), we reduced the vapor volume of 1 m <3> to about 4 liters. This process creates and holds the vacuum (7.2.1). By applying vacuum (7.2.1) of greater than -0.6 bar in the reactor (3) secondary reactions in the gas stream are avoided in order to avoid quality losses in the pyrolysis oil.

With a plant for cooling (7.9) is supplied via the coolant circuit (7.10) of the cooler to recycle cooled propellant (7.11) for the quenching process. The non-condensable and cooled fuel gases (7.13.1) leave via the line (7.12) the circulation container (7.5) and are the heat generation (8) supplied.

Through the multi-fuel burner (8.1) the heated heating medium (6.3) is fed to the reactor via the Heizmediumerhitzer (8.2) with the circulation pump (8.3). The product oil produced (7.6) leaves the circulation tank (7.5) via the product oil outlet (7.14).

The coke mixed with ash, leaves as slag (4.6) the reactor (3) via the discharge conveyor (5) and the lock (5.6). In this case, the same process takes place with the control of the gate valve (5.6), which has already been described in the lock (2).

Fig. 2 shows the reactor (3) and the condensation plant (7) concerning the application for the material entry (1) of plastic mixtures (3.15) or the processed autoshredder light fraction (3.15.1), called ASL short and catalysts (1.2), for the production of fuel oil (7.1), fuel gases (7.13) and slag (4.6).

In addition to the functional description of FIG. 2, FIG. 3 to 7 is used.

Catalysts (1.2) are added to neutralize impurities such as PVC or vulcanized rubber in which the material entry (1) for the binding of hydrogen chloride, potassium carbonate and for the binding of hydrogen sulfide, iron oxide is added.

The binding reactions are carried out at temperatures between +180 ° C to 280 ° C in the region of the reduction zone (3.8) and the melting zone (12.5). The mineral compounds are then discharged as raw materials (5.9.1) from the reactor (3).

The material entry (1) into the reactor (3) takes place cyclically via the lock (2). Thus, no atmospheric oxygen is registered, the two gate valve (2.1) are mutually locked. Shown here is a lock (2). To ensure a continuous filling, several locks (2⋅n) can be placed side by side.

After the filling of the lock (2), the content is flushed with inert gas (2.2) to displace the oxygen. After flushing the upper slide (2.1) is closed and then opened the lower slide (2.1). The lock contents fall into the feed chute (3.1) and are evenly distributed over the entire reactor width by the material distributor (3.2).

The drive (3.3) moves the auger (3.6) constantly by changing the direction of rotation (3.4) A and B, thereby distributes the registered fresh material (3.16.1) by the material distribution (3.5) alternately in the direction of A and B.

Via the drives (4.1), the material introduced is conveyed in the main flow direction (3.13) with the conveying spirals (4) The inner tube (6) is heated by the heating medium (6.3), which is enclosed by the heating jacket (6.1) and by Heating medium inlet (6.4) to the opposite heating medium outlet (6.5) flows.

By the contact of the plastic mixtures (3.15) or the treated household waste (3.16) with the hot surface of the inner tube (6), the plastic mixture (3.15) or the treated household waste (3.16) under oxygen exclusion and vacuum (7.2.1) melted at the hot contact surface. The resulting liquid film evaporates immediately and leaves as superheated steam (7.1), with a temperature between 390 to 420 ° C, via the gas dome (3.12) the reactor (3) and is via the gas line (7.1.1) the cyclone ( 10) for separating the fine dust (10.4) supplied.

Through the lock (10.1) with the slides (10.2) is passed through the outlet nozzle (10.3) of fine dust (10.4) in the discharge chute (5.5). The cleaned of the dust hot gas (10.5) is fed via the hot gas line (10.6) to the condenser.

In the packed packing condense the long-chain hydrocarbons (11.6) and are fed via the lock (11.4) and the gate valves (11.5) back to the reactor (3) for further thermal treatment.

In the temperature head (11.2), the partial temperature is adjusted via the temperature control unit (11.3) to ensure that only short-chain hydrocarbon compounds in the form of cracking gases (11.8) via the pipe (11.9) of the condensation plant (7) are supplied. Non-cracked long-chain hydrocarbon compounds (11.7) are recycled to the reactor (3) via the sluice (11.4) for re-cracking.

Fig. 3 shows a longitudinal section through a horizontally arranged reactor (3) in which the material entry (1) the residue discharge (5.9) and gas dome (3.12) is diametrically opposite and the main flow direction (3.13) from the material entry (1) in Direction Gasdom (3.12) runs.

The registered fresh material (3.16.1) is pressed through the material distributor (3.2) in the conveying spirals (4) of the melting pipes (4.7), so that in the region of the entry zone (3.7), the melting tube (4.6) is completely filled.

By the drive (4.1), the conveying spiral (4) by reversing the direction of rotation (4.2), A or B, the conveying direction (4.3) can be changed. In the direction of rotation A, the material is transported in the main conveying direction (3.13) and in the direction of rotation B in the opposite direction.

In order to regulate the passage and residence time of the melt, a step circuit is set up, which is able to perform at least one revolution in the opposite direction B after two to three revolutions in the conveying direction A.

This has the advantage that a better mixing of the melt (4.8) takes place and the contact surfaces on the heated inner tube (6) by the addition of Schleissmaterial (1.1) or Umlaufgut (1.4) and the rotational movement of the conveyor spiral (4) constantly be cleaned from caking, carbon deposits and slags (4.6) and thus ensures optimum heat input (6.6) in the melt (3.17).

By the material entry (1) of a bed of material (3.19), which already contains Schleissmaterial (1.1). Like autoshredder light fraction (3.15.1), or ASL, treated household waste (3.16), oily sludge (12.1) and oil sands (15), no wiping material (1.1) or circulating material (1.4) must be used to clean the heating surfaces of the heated inner tube (6). be added.

The admixture of catalysts is imperative if the material entry (1) contamination, e.g. in the form of gum, which releases sulfur in the form of hydrogen sulphide and PVC, which releases hydrogen chloride in the form of gases.

In case of precipitation in the reduction zone (3.8) and molten zone (12.5) in the temperature range between +180 ° C and 280 ° C with potassium carbonate, the hydrogen chloride is bound and the addition of iron oxide, the hydrogen sulfide is bound. The two elements leave the reactor (3) as a cold, dry slag (5.13) in the form of elemental sulfur and calcium chloride.

In the area of the reduction zone (3.8), the entry level (4.4) is lowered to a discharge level (4.5) by melting and gasification. Remain a residue in the slag zone (3.9), which is conveyed with the conveyor spiral (4) in the discharge zone (3.10) and on the discharge conveyor (5.1) and discharge lock (5.6) from the reactor (3) as dry material in the form of cold Slag (5.13) and residues (5.9.1) is discharged.

In the same reactor space (3.21), the following process-relevant processes take place successively: <tb> 1. <sep> The introduction of substance mixtures (3.16.2) into the entry zone (3.7) and the compression zone (12.10). <tb> 2. <sep> Melting (12.5.1) of the mixtures (3.16.2) in the melting zone (12.5) between + 200 ° and + 320 ° C. <tb> 3. <sep> Cracking (12.6.1) the molten mixtures (3.16.2) in the cracking zone (12.6) between + 320 ° and + 420 ° C under a vacuum (7.2.1) of greater than -0.5 bar , <tb> 4. <sep> Pull off the cracking gases under vacuum (7.2.1) as superheated steam (7.1) over the gas dome (3.12). <tb> 5. <sep> Dry the non-evaporated residues (5.9.1) in the drying zone (12.7) between + 320 ° C and + 420 ° C. <tb> 6. <sep> Discharge of the dry residues (5.9.1) from the drying zone (12.7) with the conveyor spiral (4) and discharge into the discharge chute (5.5).

Fig. 4 shows the section A - A through the material entry (1), the feed shaft (3.1) with the material distributor (3.2) in the juxtaposed inner tubes (6). Shown are five pieces of parallel arranged inner tubes (6), while it is possible at any time in relation to the required throughput capacity to reduce or increase the number of tubes.

Fig. 5 shows the section B - B through the middle part.

Fig. 6 shows the section C - C through the discharge zone (3.10) with the discharge conveyor (5), the discharge lock (5.6) with the outlet nozzle (10.3) for the fine dust discharge (10.4) and the gas dome (3.12).

Fig. 7 shows the top view of the adjacent reactors (3).

Fig. 8 shows the section through a reactor (3) for the flow rate of liquid products such as oily sludge (12.1) from tank farms and tankers, and oil sands (15).

The sludge (12.1) is conveyed via a transport device such as e.g. a pump (12.4) in the inner tube (6) of the reactor (3) promoted. With the delivery spiral (4), the reactor contents (12.9) are conveyed in the main flow direction (3.13) from the sludge entry (12.1) to the discharge shaft (5.5).

In both reactors (3), the melt reactor (3.1.1) and the evaporation reactor (3.1.2), the heating medium (6.3) is advantageously made of molten salt, which between the inner tube (6) and the heating mantle (6.1) in Counterflow (6.7) flows to the main flow direction (3.13) of the reactor contents (12.9).

The Heizmediumeingang (6.4) is the Heizmediumausgang (6.5) diametrically opposite. The inclination (3.18) of the reactors (3) is determined by the spiral helix height (4.9), so that the slag (4.6) can be discharged.

The length of the melt reactor (3) is divided into two zones. After the sludge entry (12.1) into the reactor (3) takes place in the melting zone (12.5), the heating of the reactor contents (12.9) to a temperature between 220 and 320 ° C, with a residence time between 1 to 3 hours. The required temperature and holding time depend on the material composition of the sludge (12.1).

The oily fractions of the sludge (12.1) are melted by the action of temperature to a honey-like mass. In the cracking zone (12.6) is due to the higher temperature between 380 ° C to 420 ° C, the reactor contents (12.9) evaporated under vacuum (7.2.1) and leaves as superheated steam (7.1) the reactor (3) via the gas dome (3.12 ).

The entry of the sludge (12.1) in the reactor (3) is effected by a level control, not shown here, which controls the level (12.8) in the reactor (3).

By the action of temperature, the long-chain hydrocarbons (11.6) are broken and converted into short-chain molecules, which after passing through the condenser (11) and the condenser condensers (7) into the fractions, fuel gases (7.13) and product oil (7.6) be converted.

In the drying zone (12.7), the residue is dried in the form of slag (4.6) at a temperature between + 400 ° and 430 ° C and a material-specific residence time between 30 minutes to 2 hours and thus by the hot inner tube (6). of the reactor (3) freed from adhering liquid. The hot slag (5.12) consists of inert material and non-cracked long-chain hydrocarbon compounds (11.7).

The residence time of the reactor contents (12.9) depends on the material composition of the fed sludge (12.1). If, in particular, low-boiling material is introduced, the residence time in the reactor (3) can be shortened and thus the throughput of sludge (12.1) can be increased. For tough slurries (12.1) with a high content of tar and heavy oil, the residence time is extended, thereby reducing the throughput per unit time.

The dried hot slag (5.12) is introduced through the conveyor spiral (4) in the discharge chute (5.5). With the discharge conveyor (5) the hot slag (5.12) via the slide (5.7) in the slag cooler (5.1) is entered. Together with the mutually locked sliders (5.7), the slag cooler (5.10) simultaneously fulfills the function of a vacuum-tight discharge sluice (5.6).

By introducing liquid nitrogen (5.11) via an upstream evaporator, a) the discharge sluice (5.6) is rendered inert and b) the hot slag (5.12) is cooled and the cold slag (5.13) is the discharge sluice (5.6) via the sluice valve (5.7) and is referred to as residue discharge (5.9).

FIG. 8.1 shows the section through a reactor (3) for the throughput of plastic mixtures (3.15).

The plastic mixture (3.15) is transported via a transport device, shown here as a delivery spiral (12.17) in the filling tube (12.18) of the reactor (3). With the delivery spiral (4), the reactor contents (12.9) are conveyed in the main flow direction (3.13) from the feed chute (3.1) to the discharge chute (5.5).

The heating medium (6.3) is advantageously made of molten salt which flows between the inner tube (6) and the heating jacket (6.1) in counterflow (6.7) to the main flow direction (3.13) of the reactor contents (12.9).

The Heizmediumeingang (6.4) is the Heizmediumausgang (6.5) diametrically opposite. The inclination (3.18) of the reactors (3) is determined by the spiral helix height (4.9) so that the hot slag (5.12) can be discharged.

The length of the reactor space (3.21) is divided into three zones. After the introduction of plastic mixture (3.15) into the reactor (3), the heating of the reactor contents (12.9) is then carried out in the melting zone (12.5) to a temperature between 220 and 320 ° C., with a residence time of between 1 and 3 hours. The required temperature and holding time depend on the material composition of the plastic mixture (3.15).

In the compression zone (12.10), the plastic mixture (3.15) introduced via the conveying spiral (12.17) is compacted by a press screw (12.12.1) and through the material flow direction (12.14) into the zone without conveying means (12.11) a plug (12.15) pressed.

This plug (12.15) prevents gases (12.16) from the melting zone (12.6) and the cracking zone (12.7) from entering the cold region of the filling tube (12.18). The gases (12.16) are forced through this device to leave the reactor (3) in the main flow direction (3.13) via the gas dome (3.12).

The compression zone (12.10) is not heated and thus prevents the cold plug (12.15) dissolves due to the action of heat.

With the spiral (4), the plug (12.15) is dug and the supplied fresh material (3.16.1) in the melting zone (12.5) and cracking zone (12.6) promoted.

In the same reactor space (3.21), the following process-relevant processes take place successively: <tb> 1. <sep> The introduction of substance mixtures (3.16.2) into the entry zone (3.7) and the compression zone (12.10). <tb> 2. <sep> Melting (12.5.1) of the mixtures (3.16.2) in the melting zone (12.5) between + 200 ° and + 320 ° C. <tb> 3. <sep> Cracking (12.6.1) the molten mixtures (3.16.2) in the cracking zone (12.6) between + 320 ° and + 420 ° C under a vacuum (7.2.1) of greater than -0.5 bar , <tb> 4. <sep> Pull off the cracking gases under vacuum (7.2.1) as superheated steam (7.1) over the gas dome (3.12). <tb> 5. <sep> Dry the non-evaporated residues (5.9.1) in the drying zone (12.7) between + 320 ° C and + 420 ° C. <tb> 6. <sep> Discharge of the dry residues (5.9.1) from the drying zone (12.7) with the conveyor spiral (4) and discharge into the discharge chute (5.5).

The oil-containing components of the plastic mixture (3.15) are melted by the action of temperature in the molten zone (12.5) at + 200 ° to 320 ° C to a honey-like mass. In the cracking zone (12.6) is evaporated by the higher temperature between 380 ° C to 420 ° C under vacuum (7.2.1) the reactor contents (12.9) and leaves as superheated steam (7.1) the reactor (3) via the gas dome (3.12 ).

When the plastic mixture (3.15) melts in the molten zone (12.6) and evaporates in the cracking zone (12.6), gas bubbles (12.16.1) are formed in the inner tube (6). Per 1000 liters of reactor volume, the formation of the gas bubbles (12.16.1) is about 50 m 3 / hour.

By rising these gas bubbles (12.16.1) in the form of superheated steam (7.1) boils the reactor contents (12.9) and thereby a continuous mixing (12.16.2) of the reactor contents (12.9) is produced.

The slowly, with a maximum of three revolutions per minute rotating conveyor spirals (4) serve to supply the fresh material (3.16.1) the heat process and the hot slag (5.12) and coke, metal and inert materials (5.12.1) in to pump the exhaust shaft (5.5).

The entry of the plastic mixture (3.15) in the reactor (3) is effected by a level control, not shown here, which controls the level (12.8) in the reactor (3).

By the action of temperature, the long-chain hydrocarbons (11.6) are broken and converted into short-chain molecules, which after passing through the condenser (11) and the condensers (7) in the fractions, fuel gases (7.13) and product oil (7.6) be converted.

When adjusting the condenser (11) to produce naphtha (12.26) with one of the hydrocarbon compounds (11.7) from C1 to C12, the fraction C6 to C12 will be at a condensation temperature below 40 ° C as a storable and transportable liquid. The non-condensable and gaseous phase, is liquefied by a cold treatment with temperatures below -65 ° C and can then be stored in approved tanks, and tank transporters and transported as LPG, similar to propane gas.

In the drying zone (12.7), the residue in the form of slag (4.6) at a temperature between + 400 ° and 430 ° C and a material-specific residence time between 30 minutes to 2 hours dried and thus by the hot inner tube (6) of the reactor (3) freed from adhering liquid. The hot slag (5.12) consists of inert material and non-cracked long-chain hydrocarbon compounds (11.7).

The residence time of the reactor contents (12.9) depends on the material composition of the supplied plastic mixture (3.15). If, in particular, low-boiling material is introduced, the residence time in the reactor (3) can be shortened and thus the throughput of plastic mixtures (3.15) can be increased. For tough plastic mixtures (3.15) with a high proportion of impurities, the residence time is increased, thereby reducing the throughput per unit time.

The dried hot slag (5.12) is introduced through the conveyor spiral (4) into the discharge chute (5.5). With the discharge conveyor (5) the hot slag (5.12) via the slide (5.7) in the slag cooler (5.1) is entered. Together with the mutually locked sliders (5.7), the slag cooler (5.10) simultaneously fulfills the function of a vacuum-tight discharge sluice (5.6).

By introducing liquid nitrogen (5.11) via an upstream evaporator, a) the discharge sluice (5.6) is rendered inert and b) the hot slag (5.12) is cooled and the cold slag (5.13) is the discharge sluice (5.6) via the gate valve (5.7) and is referred to as residue discharge (5.9).

Fig. 8.2 shows the section A - A with the view of the drive of the conveyor spirals (4).

The drive shaft (4.11) is moved by the drives (4.1, 5.2, 12.13). Attached to the drive shaft (4.11) is the outer drive star (4.12), which is moved by the rotational movement in the respective desired direction of rotation (4.2) with the toothing (4.15) of the output star (4.13) and thus the spiral (4 and 5.1 ), as well as the press screw (12.12) drives.

Due to the movement play (4.13) between the drive star (4.12) and the output stator (4.13) is the spiral (4 and 5.1), and the screw press (12.12) loose in the inner tube (6) and can adjust the bumps which by the manufacturing tolerances of the conveyor spiral (4) and the inner tube (6), and by the reactor contents (12.9), consisting of hot slag (5.12), coke, metal and inert materials (5.12.1) are caused. This prevents lateral forces on the bearing and substantially reduces the abrasion on the delivery spiral (4) and the inner tube (6).

The toothing (4.15) of the drive star (4.12) and the output star (4.13) consists of at least three pieces, distributed on the circumference toothings. Depending on the diameter of the conveyor spiral and a plurality of teeth 4.15⋅n can be attached.

It is also possible to perform the drive star (4.13) as external teeth, while the drive star (4.1) is provided with an internal toothing (4.12).

Fig. 9 shows the top view of the reactor (3) for the treatment and throughput of oily sludge (12.1).

FIG. 10 shows the treatment apparatus and method steps for the throughput of petroleum-containing and pumpable sludges (12.1).

In the mixing device, the sludge (12.1) is introduced and optionally for the addition of thinner (13.2.1) in the form of light liquid such. Kerosene made pumpable. The mixing process can be carried out as shown in a twin-shaft mixer (14.3) or another suitable mixing system.

In the event that tar- and heavy oil-containing mixtures are present, the mix (14.3) is heated via a heat input system, shown here as a circulation system with a feed pump (14.5), heat exchanger (14.6) with heating medium circuit (14.7), which the Umlaufgut (14.4) heated and as warm Umlaufgut (14.4.1) the double-shaft mixer (14.3) again supplies.

Via the viscosity and temperature control (14.11), the supply of heat via the heat exchanger (14.6) and thinner (13.2.1) via the feed pump (14.5) is controlled. In this case, advantageous pumps (14.5) are used, which are used to promote concrete.

With a loading device, represented here by an entry pump (14.9), the mix (14.8) is pressed into the mix (14.10) of the reactor (3).

By introducing over the material entry (1) of oily sludge (12.1) in the reactor (3) enough Schleissmaterial (1.1) in the form of fine sand (15.2) is introduced, therefore no Schleissmaterial (1.1) or Umlaufgut (1.4 ) are added to the material entry (1). The heat transfer surfaces of the inner tube (6) in this case, by the fine sand (15.2) contained in the sludge (12.1), constantly cleaned of caking and dirt in the form of slag (4.6).

The reactor (3) consisting of a melting tube (4.7) or more parallel or successively arranged melting tubes (4.7⋅n), the registered sludge (12.1) on the heating jacket (6.1) by the heating medium (6.3) is heated until the Cracking temperature between 350 ° C to 420 ° C was reached and leaves the reactor as superheated steam (7.1).

The residues in the form of slag (4.6) is discharged via the discharge chute (5.5) via the discharge sluice (5.6) as residue discharge (5.9) and cold slag (5.13).

In the condensation plant (7), the superheated steam is fed via the cooler, cooled by the refrigeration (7.9). The cooling temperature is adjusted so that low boilers such as kerosene leave the condensation plant (7) in the gaseous state as fuel gases (7.13) and are fed to the fuel gas cooler (13).

The product oil (7.6) leaves the container (7.5) and is adjusted via the product oil outlet (7.14) after previous cooling via the cooler (7.8) to a storage temperature of <30 ° C and applied as cooled product oil (7.6.1) ,

In the light liquid tank (7.5), the heavier water (7.19) is separated from the lighter product oil (7.6) by sinking into the water tank (7.15). With a water level measurement (7.16), shown here as a floating body, which acts on the density system, the water level is detected and discharged through the water outlet control (7.17) with the drainage pump (7.18) the water through the water outlet (7.20).

In the fuel gas cooler (13), the fuel gas (7.13) via the cooler (7.8) is cooled and the condensate is separated as light liquid (13.2) from the fuel gas (7.13) and directed into the light liquid tank (13.3). The non-condensable cooled fuel gases (7.13.1) leave the vessel (13.3) and are used as process fuel or otherwise.

The light liquid (13.2) is supplied to the mixing device (14) with a delivery device, here shown as a delivery pump (13.5) as a thinner (13.2.1). The excess of light liquid (13.2) is used as fuel (13.2.2) for process heating or other purposes.

In the case of deficiency or start of the process, light liquid (13.2) must be added via the light liquid feed (13.4) from external sources. By adding the light liquid (13.2) as a thinner (13.2.1) of the sludge (12.1) and discharge as superheated steam (7.1) from the reactor (3) in the two condensation stages, consisting of the condensation plant (7) and the fuel gas cooler ( 13), the production of the light liquid (13.2) closes the dilution cycle.

11 shows the treatment device and the process steps for obtaining hydrocarbon mixtures (15.17) from oil sands (15) by dry extraction, without adding water or steam, by heating the oil sand (15) to a cracking temperature of 380 to 420 ° C. The presented method is used for the extraction of oil sands (15) from underground and underground mining.

Before the extraction of the oil sand (15) is made free-flowing, in the lumpy material in a separation (15.1), here represented by a roll crusher to free-flowing fine sand (15.2) is processed. The fine sand (15.2) is then processed in a mixing device with its own produced thinner (13.2.1) to a moist sand mixture (15.3).

The thinner (13.2.1) consists of the light liquid obtained in the extraction process (13.2), in the form of gasoline and kerosene which is added to the fine sand (15.2) as a circulation product and extraction aid. Whether and how much thinner (13.2.1) is added to the fine sand (15.2) is determined by the toughness of the bitumen adhering to the sand grain.

The dry or moist sand mixture (15.3) is introduced via a conveying and metering device, shown here as a double-shaft mixer (14.3) in the preheating reactor (3.1.1). The heat input (6.6) into the cold sand mixture (15.4) takes place via the heating surface of the inner tube (6).

The heating medium (6.3) consists of a thermal oil circulation by using the Heizmediumumwälzpumpe (15.4) via the heat exchanger tubes (15.11) in Rieselbettreaktor (15.12) the approximately 400 ° C hot sand (15.6), heat is removed and the Heizmediumvorlauf ( 15.15) and heating medium return (15.16), the heat exchanger of the preheating reactor (3.1.1) is heated.

The warm sand mixture (15.5) at about 150 ° C is introduced from the reactor (3.1.1) in the reactor (3). The inclination (3.18) is set to the spiral helix height (4.9), so that it is achieved that when pumped into the main flow device (3.13), about 50% of the hot sand (15.6) constantly bends over and thus back mixing (15.6.1) takes place and constantly new surfaces, as well as the hot inner tube (6), as well as on the surface which is exposed to the vacuum (7.2.1) form.

By in the oil sand (15) enough Schleissmaterial (1.1) is in the form of sand, no cleaning aid to keep free the heating surfaces of the inner tube (6) in the form of Schleissmaterial (1.1) or Umlaufgut (1.4) must be added.

By baking the hot sand (15.6) at about 400 ° C to 430 ° C, the oily components go into a gas phase and leave the reactor (3) as superheated steam (7.1). The equally hot, but freed from the oily organics sand, leaves as dehumidified sand (15.7) the reactor (3) and passes through the discharge conveyor (5) in the discharge lock (5.6) and is to cool the material distribution (15.10) the trickle bed reactor (15.12) supplied.

After passing through the trickle bed reactor (15.12) heat is removed from the hot and dehumidified sand (15.7) via the heat exchanger tubes (15.11) and leaves the reactor (15.12) via the discharge device (15.12) as cool sand (15.8) and this can then be returned as backfill material (15.9) to the oil sands extraction site.

The cracking gases leave as superheated steam (7.1) the reactor (3) via the gas dome (3.12) and enter the cyclone (10) in which fine dust (10.4) are separated from the hot gas before they are fed into the condenser (11) become. In this first selective partial condenser long-chain and not cracked hydrocarbons are excreted in liquid form and fed via the lock (11.4) back to the reactor (3) for re-cracking.

The cleaned cracking gases (11.8) aspirated from the vacuum (7.2.1) enter the liquid jet pump (7.2) and are abruptly cooled by the propellant liquid (7.3). The cooled propellant (7.11) consists of the product oil (7.6) which from the circulation tank (7.5) by means of the circulation pump (7.7) via the cooler (7.8) in turn drives the liquid jet pump (7.2) and at the same time the vacuum (7.2.1) and Cooling cracking gases (11.8) and condensing to product oil (7.6).

The co-condensed water vapor is collected as water (7.19) in the water tank (7.15) and withdrawn via Wasserabzugssteuerung (7.16 and 7.17) with the dewatering pump (7.17).

The product oil (7.6) with a temperature of approx. + 60 ° C leaves the process via the cooler (7.8) with cooling (7.9) as cooled product oil (7.6.1). The non-condensable fuel gases (7.13) and low-boiling gaseous Liquids are the fuel gas cooler (13) supplied and cooled in this via the cooler (7.8), fed on the refrigeration (7.9), from about 70 ° C to 30 ° C and condensed to liquid fuel (13.2).

The non-condensable cooled fuel gases (7.13.1) leave the fuel gas cooler (13) and are burned in the multi-fuel burner (8.1) in the heat generation (8) for heating the heating medium (6.3).

If necessary, the light liquid 13.2 is fed via the pump (13.5) as diluent (13.2.1) and solvent to the mixing device (14). The excess of light liquid can be supplied as fuel (13.2.2) to the process or other energy consumers.

When starting the extraction plant or in the absence of circulating liquid in the form of thinner (13.2.1) light liquid (13.4) in the form of kerosene or gasoline must be supplied.

FIG. 11.1 shows a longitudinal section as a cut through the melt reactor (3.1.1) and the reactor (3). Shown here is the back mixing 15.6.1, which is determined by the angle of attack of the inclination (3.18) and the spiral spiral height (4.9) of the conveyor spiral (4), as well as the amount of metered material entry (1 and 15).

Fig. 11.2 shows the section A-A as embodiment 1 with adjacent, closed reactors (3) and preheating reactor (3.1.1).

11.3 shows the section AA as a variant 2 with adjacent, open-topped reactors (3) and melt reactors (3.1.1) in which the inner tube (6) as a half-pipe and the heating jacket (6.1) formed as a trough is. The degassing chamber (3.11) is closed with the gas-tight cover (3.20).

12 shows the treatment device and process steps in a cascaded arrangement of the reactor (3) and consists of a melt reactor (3.1.1) and an evaporation reactor (3.1.2), which together via the entry shaft (5.5.1) are connected to a reactor space (3.21). This arrangement is used in the material entry (1) of heavily contaminated with organic material (1.5) and abrasive mixtures as in the treatment of autoshredder light fractions (3.15.1), in which there are also PVC residues, broken glass, non-ferrous metals and inorganic substances ,

The plastic mixture (3.15) is conveyed via a transport device, here represented as a delivery spiral (12.17) into the filling tube (12.18) of the reactor (3). With the delivery spiral (4), the reactor contents (12.9) are conveyed in the main flow direction (3.13) from the feed chute (3.1) to the discharge chute (5.5).

The heating medium (6.3) is advantageously made of molten salt which flows between the inner tube (6) and the heating jacket (6.1) in countercurrent (6.7) to the main flow direction (3.13) of the reactor contents (12.9).

The Heizmediumeingang (6.4) is the Heizmediumausgang (6.5) diametrically opposite. The inclination (3.18) of the reactors (3) is determined by the spiral helix height (4.9), so that the slag (4.6) can be discharged.

In the series connection of the first reactor is operated as a melt reactor (3.1.1) at an operating temperature between +250 ° C to +320 ° C for melting the plastic components in the molten zone (12.5).

The flowable melt (3.12) flows via the feed shaft (5.5.1) into the downstream evaporation reactor (3.1.2). The mixed gases (7.12) are withdrawn via the gas dome (3.1.1) and sent for thermal utilization.

The two reactors (3.1.1 and 3.1.2) have the same slope (3.18). The upper level (12.8.1) limits the cracking zone (12.6) in the reactor (3.2.1). In the drying zone (12.7), the supernatant and the slag (4.7) are dried by the heat input and fed via the discharge chute (5.5) of the discharge lock (5.6).

The operating temperature in the reactor is between 380 ° C to 420 ° C. The cracking gases leave as superheated steam (7.1) under vacuum (7.2.1) the reactor (3) via the gas dome (3.12) for further treatment in the downstream treatment stages, consisting of cyclone (10), condenser (11) and condensation plant (7) to liquid hydrocarbons.

In both reactors (3), the melt reactor (3.1.1) and the evaporation reactor (3.12), the heating medium (6.3) advantageously consists of molten salt, which between the inner tube (6) and the heating mantle (6.1) in countercurrent ( 6.7) flows to the main flow direction (3.13) of the reactor contents (12.9).

The Heizmediumeingang (6.4) is the Heizmediumausgang (6.5) diametrically opposite. The inclination (3.18) of the reactors (3) is determined by the spiral helix height (4.9) so that the hot slag (5.12) can be discharged.

The length of the reactor (3.1.1) is divided into two zones. After the introduction of plastic mixture (3.15) into the melt reactor (3.1.1), the reactor contents (12.9) are then heated in the melt zone (12.5) to a temperature between 220 and 320 ° C., with a residence time of between 1 and 3 hours. The required temperature and holding time depend on the material composition of the plastic mixture (3.15).

In the compression zone (12.10), the plastic mixture (3.15) introduced via the delivery spiral (12.17) is compressed by a press screw (12.12) and through the material flow direction (12.14) into the zone without conveying means (12.11) to form a plug (12.15). pressed.

This plug (12.15) prevents gases (12.16) from the melting zone (12.6) and the cracking zone (12.7) from entering the cold region of the filling tube (12.18). The gases (12.16) are forced through this device to leave the reactor (3) in the main flow direction (3.13) via the gas dome (3.12). The applied vacuum (7.2.1) supports this degassing process.

The compression zone (12.10) is not heated and thus prevents the cold plug (12.15) dissolves due to the action of heat.

With the slide (12.19), each reactor (3) can be controlled individually and shut off against the material inlet (1) and the backflowing material from the melting zone (12.5).

Shown here is a plate slide with a slide plate (12.20) and a slide drive (12.21). It is possible to use other suitable shut-off.

By means of the slide (12.19) reactors (3) can be switched on or off with quantitative variations in the material input (1) without the heating medium (6.3) consisting of molten salt being switched off.

With the conveyor spiral (4), the plug (12.15) is dug and the supplied fresh material (3.16.1) conveyed into the molten zone (12.5).

The oily portions of the reactor contents (12.9) are melted by the action of temperature to a honey-like, flowable mass, which flow at the end of the melt reactor as a melt (3.1.7) in the feed shaft (5.5.1).

In the feed shaft (5.5.1), the mixed gases (7.1.2) separate from the melt (3.17) and the melt (3.17) is fed to the evaporation reactor (3.1.2).

Due to the effect of temperature between + 400 ° to 420 ° C in the cracking zone (12.6), the long-chain hydrocarbons (11.6) broken and converted into short-chain molecules, which are discharged as superheated steam (7.1) under vacuum (7.2.1) and after passing through the condenser (11) and the condenser condensers (7), they are converted into the fractions, fuel gases (7.13) and product oil (7.6).

In the drying zone (12.7), the residue in the form of hot slag (5.12) at a temperature between + 400 ° and 420 ° C and a material-specific residence time between 30 minutes to 2 hours dried and thus by the hot inner tube (6 ) of the evaporation reactor (3) by means of the shear forces of the delivery spiral (4) freed from adhering liquid. The hot slag (5.12) consists of inert material and non-cracked long-chain hydrocarbon compounds (11.7).

The residence time of the reactor contents (12.9) depends on the material composition of the supplied plastic mixture (3.15). If, in particular, low-boiling material is introduced which shortens the residence time in the reactor (3), the throughput of plastic mixtures (3.15) can be increased. For tough plastic mixtures (3.15) with a high proportion of impurities, the residence time is increased, thereby reducing the throughput per unit time.

The dried hot slag (5.12) is introduced through the conveyor spiral (4) into the discharge chute (5.5). With the discharge conveyor (5) the hot slag (5.12) via the slide (5.7) in the slag cooler (5.1) is entered. Together with the mutually locked valves (5.7), the slag cooler (5.12) simultaneously fulfills the function of a vacuum-tight discharge sluice (5.6).

By introducing liquid nitrogen (5.11) via an upstream evaporator, a) the discharge sluice (5.6) is rendered inert and b) the hot slag (5.12) is cooled and, as cold slag (5.13), the discharge sluice (5.6) via the gate valve (5.7) and is referred to as residue discharge (5.9).

The fill level (12.8) in the melt reactor (3.1.1) and in the evaporation reactor (3.1.2) are measured via the fill level difference (12.22) in the feed shaft (5.5.1). As a result of the evaporation of the reactor contents (12.9) in the cracking zone (12.6), the level in the evaporation reactor (3.1.2) and in the inlet shaft (5.5.1) drops from the upper level (12.8.1) to the lower level (12.8.2).

Since in the entry shaft (5.5.1) no internals such as e.g. Stirring elements, the level difference (12.22) via a pressure transducer (12.23) with evaluation and control unit via the differential pressure (12.24) is measured.

The actuators (12.13 and 4.1) are actuated with the control signal (12.25), and the slide drive (12.21) is opened so that the contents of the reactor (12.9) are refilled via the material entry (1) until the upper fill level (12.8. 1) in the entry shaft (5.5.1) is reached again. This shuts off the drives (12.13 and 4.1) and closes the slide drive (12.21). Instead of a differential pressure measurement, other suitable measuring systems can be used.

The 280 to 320 ° C hot mixed gases (7.1.2) from the feed shaft (5.5.1) are collected in the gas dome (3.12) and fed into the horizontal conveyor (18.13). The mixed gases (7.1.2) from the melt reactor (3.11) contain paraffin (18.1) which precipitate on the walls of the spiral conveyors (18.16) and build up.

By continuously rotating the conveyor spirals (4) in the spiral conveyor (18.16) in the main flow direction (3.13), the paraffin (18.1) is scraped off the walls of the spiral conveyor (18.16) and transported to the feed pump (18.2). The mixed gases can thereby pass unhindered through the center opening (4.10) of the conveyor spiral (4) in the gas line (18.15).

The vertical conveyor (18.14) is provided with coolers (7.8), which cools the wall of the vertical conveyor (18.14) via a coolant circuit (7.10).

The mixed gases (7.1.2) which reach the cooled vertical conveyor (18.14) at a temperature of +280 to 320 ° C via the horizontal conveyor (18.13) are cooled to +90 to 120 ° C.

The paraffin (18.1) precipitates and settles as a soft wax on the walls of the spiral conveyors as paraffin fraction (18.1.1) down. The water vapor contained in the mixed gas (7.1.2), as well as fuel gases, are fed as water vapor and gas fraction (18.18.1) via the gas line (18.15) to the gas scrubber (18.4).

The paraffin (18.1) is pressed at the lower end of the vertical conveyor (18.14) through the conveyor spiral (4) in the feed pump (18.2). The feed pump (18.2) is shown as a gear pump. It is also possible to use other suitable feed pumps (18.2).

The feed pump (18.2) presses the compacted paraffin (18.1) via the pressure line (18.3) into the evaporation reactor (3.1.2). The paraffin (18.1) mixes with the liquid reactor content, which is approximately 400 ° C (12.9), and leaves the evaporation reactor (3.1.2) via the gas dome (3.1.2) as superheated steam (7.1).

The water vapor and gases (7.1.3) from the separation plant (18) pass via the gas line (18.15) into the gas scrubber (18.4).

In the material entry (1) of the crop (1.5) which may contain PVC or vulcanized rubber, as well as organics in the form of food adhesions, go at a pyrolysis between +220 to 320 ° C these aforementioned substances, in a gaseous state.

For PVC, the chloride content is min. 52%, which is then expelled as gaseous hydrogen chloride. Vulcanized rubber releases hydrogen sulphide. Most food residues release butyric acid. These acidic gases are neutralized in the alkaline gas scrubber (18.4) by passing the acidic water vapor and gases (7.13) through the surface-enlarging packing, which is wetted from above with the alkaline scrubbing liquid (18.7) via the spray device (18.9).

The washing liquid (18.7) circulates in the container (18.5) and is sucked by the circulation pump (18.8) and cooled to <40 ° C via the cooler (7.8). The cooled circulating liquid (18.17) is used to cool the acidic water vapor and the gases, and the condensable fractions are passed as condensate (18.12) into the washing liquid (18.7).

The PH regulation takes place via the PH control (18.11) and the associated dossier station (18.10) with which the PH value is raised via the introduction of caustic soda. The non-condensable gases leave the gas scrubber (18.4) as fuel gases (7.1.4).

The supernatant liquid (18.18) is separated in the light liquid separation plant (18.19) into the constituents, light liquid (18.20) in the form of liquid fuel, such as a) gasoline, acetone and b) water (18.21) for further treatment in a sewage treatment plant.

Fig. 12.1 shows a section A-A through the vertical conveyor (18.14) and the conveyor spiral (4). Through the center opening (4.10), the water vapor and gases (7.1.3) can circulate freely and the caking of paraffin (18.1) are scraped off by the conveyor spiral (4) and transported to the feed pump (18.2).

FIG. 12.2 shows the treatment apparatuses and method steps in a cascaded arrangement of the reactor space (3.21), with an upstream drying stage (19) for the treatment of mechanically treated domestic waste (3.16). FIGS. 12 and 12.1 describe the functions of the preheating / melting reactor (3.1.1) and of the evaporation reactor (3.1.2).

The mechanically treated domestic waste (3.16) comes from the fraction screen overflow with a water content of 10 to 20% and a grain size of greater than 80 mm and is comminuted before entry in the dryer (19) on a small grain 40 mm. This recycled domestic waste (3.16) is introduced via the feed chute (3.1) at the lower end of the dryer (19) by means of a conveyor spiral (12.17).

The dryer consists of an inner tube (6), comprising a heating jacket (6.1) in which a heating medium (6.3) flows in countercurrent (6.7) to the main flow direction (3.13), consisting of compressed hot water or other suitable heating medium (6.3) with a temperature of + 110 ° C.

The Heizmediumausgang (6.5) is located directly next to the feed chute (3.1) and the Heizmediumeingang (6.4) is located immediately adjacent to the melt reactor entry (19.2).

The moist domestic waste fraction (12.9.1) is conveyed from the feed chute (3.1) in the main flow direction (3.13) to the melt reactor inlet (19.2) by the feed spiral (4) and mixed through the backmixing (15.6.1) (see FIG. 11.1 ).

The backmixing (15.6.1) constantly creates new surfaces in the moist household waste fraction (12.9.1), which is heated by the hot inner tube (6) to a temperature of + 110 ° C. (6.7.1) and conduct the released water vapor (19.1) via the gas dome (3.12) into an exhaust air treatment (19.3).

The exhaust air treatment (19.3) can consist of a biofilter system or also of an exhaust scrubber and condenser. The odor-activated and dehumidified exhaust air (19.3) is released into the atmosphere. The condensate (19.5) is introduced into a wastewater treatment plant.

The dried domestic waste fraction (12.9.4) is conveyed via the melt reactor entry (19.2) into the melt reactor (3.1.1), which is operated at a temperature of +300 ° C. (6.7.2) and the fused household waste fraction (12.9. 2) consisting of molten plastic mixture (3.15) mixed with coke (5.15) from the materials, paper, cardboard, leather, textiles, wood and pulp is fed as a mixture to the evaporation reactor (3.12) via the entry shaft (5.5.1).

In the evaporation reactor (3.1.2), the mixture of coke and liquid (12.9.3) over the heating medium (6.3) is heated to a temperature of + 400 ° C. As a result, the molten plastic mixture (3.15) evaporates and, as superheated vapor (7.1), leaves the evaporation reactor (3.1.2) under vacuum (7.2.1) via the gas dome (3.12).

In the drying zone (12.7), the solid components in the form of coke, metal and inert substances (5.12.1) as dry matter via the discharge chute (5.5) and the discharge conveyor (5) and slag cooler (5.10) as cold slag ( 5.13) into the slag preparation (5.14).

In slag processing (5.14), the input material is granulated and processed into product streams via mechanical and electronic treatment steps and leaves the plant as coke (5.15), metals (5.16) and inert materials (5.17).

The coke (5.15) which originates from the high-calorific components of the treated domestic waste (3.16) and in the reactor (3), consisting of the treatment stages, dryer (19), melt reactor, (3.11) and evaporation reactor (3.12), after the slag treatment (5.14) in a methanol production (5.18), not shown, the coke (5.15) to methanol (5.19) converted. The methanol (5.19) can be used in internal combustion engines as a fuel, as well as directly in fuel cells as an energy source.

Fig. 13 shows the reactor (3) in the combination of a melt reactor (3.1.1) and evaporation reactor (3.1.2) with direct firing on the multi-fuel burner (8.1 and 8.1 * n), which as fuel energy with the fuel gases (7.1.3) and the product oil (7.8).

The multi-fuel burners (8.1 and 8.1⋅n) heat with their heat energy (6.10) directly the heat plate (6.12) of the heating mantle (6.1). The heating jacket (6.1) encloses the inner tubes (6.1 and 6.1⋅n), which are immersed in a heating medium (6.3). The heating medium level (6.9) is above the inner tubes (6.1 and 6.1⋅n). Between the heating medium level (6.9) and the upper part of the heating jacket (6.1), there is an expansion space (6.13) for the thermal expansion of the heating medium (6.3).

The heating medium (6.3) as a heat carrier, advantageously consists of a thermosalt mixture based on sodium chloride, with a melting point at about 160 ° C and a boiling point above 850 ° C.

The entire closed heating jacket (6.1) with the heating plate (6.12) and the inner tubes (6 and 6⋅n) and the heating medium (6.3) is comprised of a flue gas space (8.6), which in turn is covered by the boiler shell (6.8).

The registered thermal energy (6.10) acts directly on the hot plate (6.12) and the hot flue gases (6.11 and 8.5) guided in the flue gas space (8.6) wash around and heat the entire heating mantle (6: 1). By the heat input (6.6.1), the heating medium (6.3) is heated and liquefied and distributed the registered heat energy evenly. The heating medium (6.3) in turn heats the bed of material (3.19) in the inner tube (6 and 6⋅n) by the heat input on all sides (6.6).

The bed of material (3.19) is melted at about 220 ° C and evaporated at about 400 ° C and leaves as superheated steam (7.1) the reactor (3). The residues and slag (6), with the conveyor spiral (4) in the main flow direction (3.13) to the discharge shaft (5.5) promoted.

FIG. 14 shows a cross-section AA through the reactor (3 and 3.1.1) according to FIG. 13. Shown are five pieces of inner tubes (6 and 6⋅n) enclosed by a heating jacket (6.1) with an underlying heating plate (FIG. 6.12).

The closed inner container (6.14) is filled with the heating medium (6.3) except for the expansion space (6.13). The inner container (6.14) is in turn enclosed with the boiler shell (6.8). The flue gas chamber (8.6) between the two containers serves to introduce heat (6.6.1) via the hot flue gases (6.11) into the heating medium (6.3). The flue gases (6.11) leave the reactor (3) and the preheating reactor (3.1.1) via the exhaust stack (8.4) as exhaust gases (8.5).

This indirect firing of the inner tube (6 and 6⋅n) of the reactor (3) and preheating reactor (3.11) with an open flame from the multi-fuel burner (8.1 and 8.1.2) via a heating medium (6.3) prevents punctual overheating and evened out the Entry of heat energy (6.6).

Fig. 15 shows a PET recovery plant (16) consisting of apparatuses for carrying out a process with which, after the preceding cracking operation, the purified hot gas (10.5) is recovered by partially cooling the terephthalic acid as a crystalline PET powder (16.1) can be. The PET powder (16.1) is then returned to PET production.

The freed of flues and purified hot gas (10.5) from the reactor (3) is passed through the hot gas supply (16.14) at a temperature of about 400 ° C in the PET recovery system (16). The hot gas velocity (16.25) in the hot gas supply (16.14) depends on the cross section (16.20) and the amount of gas and is in this range <3.0 m / sec.

In the screw conveyor (16.3) with center tube (16.4) results from the pitch of the screw helix (16.5) an annular gap channel cross section (16.24), which defines the hot gas velocity (16.25) by its dimensioning together with the reactor cross-section (16.21).

The hot gas velocity (16.25) in the annular gap cross-section (16.24) or annular gap channel is ideally below 0.2 m / sec. Thus, with the low gas velocity (16.8), the inlet temperature of the hot gas (10.5) is cooled from approximately 400 ° C over the surface of the cooling tube (16.8) and in the region of the constriction (16.8.1) the gas temperature is still Max. at +350 ° C.

By the cooling medium (16.10) in the double jacket (10.9) which precedes in countercurrent to the flow direction (16.11) to the conveying direction (16.6), the surface of the cooling tube (16.8) is cooled and the temperature difference of about 50 ° C causes the Reaction that the terephthalic acid in the hot gas (10.5) precipitates as PET powder (16.1) and precipitates on the wall of the cooling tube (16.8) and builds up a layer, which is then rotated by the screw conveyor (16.3) with the direction of rotation (16.7) and conveying direction (16.6) for constriction (16.8.1) is promoted.

By the constriction (16.8.1) results in a reduced cross section (16.22) and thereby a high gas velocity (16.19) which should ideally be between 8 to 15 m / sec to the scraped PET powder (16.1) with the high Gas velocity to transport to a dust separation plant, here shown as a cyclone separator (16.16). It is also possible to discharge and separate the PET powder (16.1) in a hot gas filter dust unit (not shown here).

After the cyclone separator (16.16), the hot gas (10.5.1) ignited by the PET powder (16.1) leaves the PET recovery plant (16) via the enlarged cross section (16.23) with a low gas velocity of approx. <0.3 m / sec.

Adapted to the volume flow of purified hot gas (10.5) several PET recovery systems (16⋅n) can be connected side by side or in series.

Fig. 16 shows the section A-A through the PET recovery plant.

Fig. 17 shows a section of the heat transfer surface for performing the ablative flash pyrolysis. The heating surface (17.4) is surrounded by a heating jacket (6.1) in which a heating medium (6.3) flows, which has a high heat density and advantageously consists of molten salt.

FIG. 18 shows an evaporation device (17) for the throughput of biomass (3.14) in the form of chopped straw or wood chips, as well as mechanically treated domestic waste (3.16).

Via the material entry (1), the feed material (17.15) is pressed into the screw worm (17.8) with the conveying spiral (4). This loading process can also take place via a loading device, not shown here, such as e.g. with a piston press similar to a concrete pump.

Via the drive (4.1), the screw worm (17.8) presses the crop (17.15) against the heating surfaces (17.4) of the outer cone (17.2). The cone angle (17.7) depends on the bulkiness of the input material and is ideally between 20 and 45 °. Due to the material pressure (17.9), the surface pressure (17.10) on the heating surface (17.4) is between 4 and 10 kg / cm 2.

The superheated steam (7.1) leaves the reactor space (3.21) via the degassing channels (17.16) and the gas dome (3.12). In the gas dome (3.12), the heavy slag (4.6) falls into the discharge conveyor (5) and is conveyed via the discharge spiral (5.1) to the residue discharge (5.9).

The compacted material, consisting of biomass (3.14) in the form of straw and wood chips and processed household waste (3.16) and is pressed against the heating surface (17.4) with a surface pressure (17.10) of 4 to 10 kg per cm2. Due to the effect of temperature of 450 to 550 ° C, a melting zone (17.11) and directly to the heating surface (17.4) forms an evaporation zone (17.12).

In the evaporation of biomass (3.14) and household waste (3.16) in the molten zone (17.11) and the material pressure zone (17.9) despite high surface pressure (17.10) by the lumpiness of the material distribution enough degassing channels (17.16) available to help the vacuum or vacuum (7.2.1) to ensure degassing.

Due to the absence of oxygen, a pyrolysis process takes place, which is basically comparable to a retort gasifier for producing water gas from coal. In contrast to the urban gas production process, water does not need to be added to form hydrogen in the process presented here, as there is enough moisture in the biomass (3.14) and domestic waste (3.16). Also, the ablative flash pyrolysis process presented here proceeds in a so-called low temperature range between 450 and 550 ° C.

In the evaporation of lignin-containing substances from the biomass (3.14) is obtained after cooling in the condensation plant (7), fuel gases (7.13) and wood oil (3.14.1) as fuel (7.6). The fuel gases (7.1.4) and the coke (5.15) are burned to generate the process energy in the heat generation (8).

In the pyrolysis of treated domestic waste (3.16), an electrostatic precipitator (7.21) is used for fine dust separation in the hot gas stream (7.1), provided with a discharge lock (7.22) for discharging the fine dust fraction (7.23). This fine dust fraction (7.23) is burned together with the combustible fraction from the waste material discharge (5.9) in a thermal oxidation (not shown here) with the addition of technical oxygen and the vitrified slag is deposited.

FIG. 19 shows a variant embodiment of the arrangement of the heating surfaces (17.4) in combination with an outer cone (17.2) and a heating surface (17.4) in the extension of the guide casing (17.13).

FIG. 20 shows an alternative embodiment of the arrangement of the heating surfaces (17.4) in combination with an outer cone (17.2) and an inner cone (17.1).

Fig. 21 shows a variant of the arrangement of the heating surfaces (17.4) as a straight plate heater (17.3).

FIG. 22 shows a variant of FIGS. 2, 3, 12 and 14 in which plastic mixtures (3.15) and auto-shredding light fraction (3.15.1) are vaporized with the evaporation device (17).

By cooling the guide casing (17.13) by the cooler (7.8) and the coolant circuit (7.10) in the shaft of the screw screw (17.18) via the rotary distributor (17.14) prevents radiation heat (17.17) softens the plastic fraction and thus the pressure build-up affected in the material pressure zone (17.9).

Here, shown as a heating surface (17.4) an outer cone (17.2) with the possibility that also heating surfaces (17.4) as described in FIGS. 19 to 21, can be used.

FIG. 23 shows the heat generation (8) for heating the reactors (3). Instead of using a gas burner or multi-fuel burner (8.1) the self-produced, cooled fuel gas (7.13.1) is used to drive a gas turbine (8.7) which drives a generator (8.8) to generate electricity and with the +700 ° C hot hot gases (8.10) at the same time the heat generation (8) supplied with heating energy.

In the flue gas chamber (8.6), the thermal salt is heated via the heating medium heater (8.2), which flows through the heating medium inlet (6.4) and heating medium outlet (6.5) through the heating medium heater (8.2).

The design of the gas turbine (8.7) with respect to the efficiency is carried out to generate high exhaust gas temperatures in the hot gas (8.10) to the detriment of the optimal generation of electrical energy (8.9).

Despite this shift in favor of hot gas generation, all of the electrical and thermal process energy can be met from the proprietary fuel gases.

LIST OF REFERENCE NUMBERS

[0221] <tb> A <sep> turning and conveying direction <tb> B <sep> Rotation and conveying direction <Tb> 1 <sep> Material entry <Tb> 1.1 <sep> Schleissmaterial <Tb> 1.2 <sep> Catalysts <tb> 1.3 <sep> Screening and separating device <Tb> 1.4 <sep> circulation material <Tb> 1.5 <sep> Eintragsgut <Tb> 2 <sep> sluice <Tb> 2.1 <sep> Gate Valve <Tb> 2.2 <sep> inert gas <Tb> 3 <sep> reactor <tb> 3⋅n <sep> Several reactors <Tb> 3.1 <sep> insertion slot <Tb> 3.1.1 <sep> melting reactor <Tb> 3.1.2 <sep> evaporation reactor <Tb> 3.2 <sep> Material distributor <Tb> 3.3 <sep> Drive <Tb> 3.4 <sep> rotator <Tb> 3.5 <sep> material distribution <Tb> 3.6 <sep> auger <Tb> 3.7 <sep> entry zone <Tb> 3.8 <sep> reduction zone <Tb> 3.9 <sep> slag zone <Tb> 3.9.1 <sep> drying <Tb> 3.10 <sep> discharge zone <Tb> 3.10.1 <sep> discharge <Tb> 3.11 <sep> degassing <Tb> 3.12 <sep> gas dome <Tb> 3.13 <sep> main current direction <Tb> 3.14 <sep> Biomass <Tb> 3.14.1 <sep> Fuel Oil <Tb> 3.15 <sep> plastic mixture <tb> 3.15.1 <sep> Autoshredder light fraction (short name ASL) <tb> 3.16 <sep> Recycled household waste <Tb> 3.16.1 <sep> fresh material <Tb> 3.16.2 <sep> mixtures <Tb> 3.17 <sep> melting <Tb> 3.18 <sep> inclination <Tb> 3.19 <sep> material fill <tb> 3.20 <sep> Gas-tight cover <Tb> 3.21 <sep> reactor chamber <Tb> 4 <sep> spiral conveyor <Tb> 4.1 <sep> Drive <Tb> 4.2 <sep> direction of rotation <Tb> 4.3 <sep> conveying direction <Tb> 4.4 <sep> entry level <Tb> 4.5 <sep> Austragsniveau <Tb> 4.6 <sep> slag <Tb> 4.7 <sep> melting tube <Tb> 4.7⋅n <sep> melting pipes <Tb> 4.8 <sep> melting <Tb> 4.9 <sep> spiral coil height <Tb> 4.10 <sep> Center opening <Tb> 4.11 <sep> Drive Shaft <Tb> 4.12 <sep> Drive Star <Tb> 4.13 <sep> output Stern <Tb> 4.14 <sep> motion <Tb> 4.15 <sep> Gear <tb> 4.15⋅n <sep> multiple gears <Tb> 5 <sep> discharge conveyor <Tb> 5.1 <sep> Austragsspirale <Tb> 5.2 <sep> Drive <Tb> 5.3 <sep> direction of rotation <Tb> 5.4 <sep> conveying direction <Tb> 5.5 <sep> discharge chute <Tb> 5.5.1 <sep> entry shaft <Tb> 5.6 <sep> airlock <Tb> 5.7 <sep> Gate Valve <Tb> 5.9 <sep> Reststoffaustrag <Tb> 5.9.1 <sep> residual materials <Tb> 5.10 <sep> slag cooler <Tb> 5.11 <sep> Liquid Nitrogen <tb> 5.12 <sep> Hot slag <tb> 5.12.1 <sep> Coke, metal and inert materials <tb> 5.13 <sep> Cold slag <Tb> 5.14 <sep> slag processing <Tb> 5.15 <sep> coke <Tb> 5.15.1 <sep> Pyrolsysekoks <Tb> 5.16 <sep> Metals <Tb> 5.17 <sep> inert substances <Tb> 5.18 <sep> methanol production <Tb> 5.19 <sep> Methanol <Tb> 6 <sep> inner tube <tb> 6⋅n <sep> Several inner tubes <Tb> 6.1 <sep> heating jacket <Tb> 6.3 <sep> heating medium <tb> 6.4 <sep> Heating medium input <tb> 6.5 <sep> Heating medium output <Tb> 6.6 <sep> heat input <Tb> 6.6.1 <sep> heat input <Tb> 6.7 <sep> countercurrent <tb> 6.7.1 <sep> Temperature +110 ° C <tb> 6.7.2 <sep> Temperature +300 ° C <tb> 6.7.3 <sep> temperature +400 ° C <Tb> 6.8 <sep> boiler casing <tb> 6.9 <sep> heating medium level <Tb> 6.10 <sep> thermal energy <tb> 6.10.1 <sep> Open flame <Tb> 6.11 <sep> fumes <Tb> 6.12 <sep> hot plate <Tb> 6.13 <sep> expansion space <Tb> 6.14 <sep> inner container <Tb> 7 <sep> condensation plant <tb> 7.1 <sep> Superheated steam <Tb> 7.1.1 <sep> gas line <Tb> 7.1.2 <sep> mixed gases <tb> 7.1.3 <sep> Water vapor and gases <Tb> 7.1.4 <sep> combustion gases <Tb> 7.2 <sep> liquid jet pump <Tb> 7.2.1 <sep> vacuum <Tb> 7.3 <sep> motive liquid <Tb> 7.4 <sep> mixture <Tb> 7.5 <sep> circulation container <Tb> 7.6 <sep> Fuels <tb> 7.6.1 <sep> Refrigerated product oil <Tb> 7.7 <sep> circulation pump <Tb> 7.8 <sep> cooler <Tb> 7.9 <sep> refrigeration <Tb> 7.10 <sep> coolant circuit <tb> 7.11 <sep> Cooled propellant <Tb> 7.12 <sep> gas line <Tb> 7.13 <sep> combustion gases <tb> 7.13.1 <sep> Cooled fuel gases <Tb> 7.14 <sep> product oil disposal <Tb> 7.15 <sep> water tank <Tb> 7.16 <sep> water level measurement <Tb> 7.17 <sep> water discharge control <Tb> 7.18 <sep> drainage pump <Tb> 7.19 <sep> Water <Tb> 7.20 <sep> water outlet <Tb> 7.21 <sep> electrostatic precipitator <Tb> 7.22 <sep> airlock <Tb> 7.23 <sep> particulate fraction <Tb> 8 <sep> heat generation <Tb> 8.1 <sep> multifuel <tb> 8.1⋅n <sep> Several multi-fuel burners <Tb> 8.2 <sep> Heizmediumerhitzer <Tb> 8.3 <sep> Circulation <Tb> 8.4 <sep> exhaust stack <Tb> 8.5 <sep> exhaust <Tb> 8.6 <sep> flue gas space <Tb> 8.7 <sep> Gas Turbine <Tb> 8.8 <sep> Generator <tb> 8.9 <sep> Electrical energy <Tb> 8.10 <sep> hot gases <Tb> 9 <sep> casing <Tb> 9.1 <sep> Level <Tb> 9.2 <sep> gas chamber <Tb> 10 <sep> cyclone <Tb> 10.1 <sep> sluice <Tb> 10.2 <sep> Gate Valve <Tb> 10.3 <sep> outlet spigot <Tb> 10.4 <sep> Particulates <tb> 10.5 <sep> Purified hot gas <Tb> 10.6 <sep> Hot gas line <Tb> 11 <sep> capacitor <Tb> 11.1 <sep> random packing <Tb> 11.2 <sep> Temperierkopf <Tb> 11.3 <sep> temperature control <Tb> 11.4 <sep> sluice <Tb> 11.5 <sep> Gate Valve <tb> 11.6 <sep> Long-chain hydrocarbons <tb> 11.7 <sep> Long-chain hydrocarbon compounds <Tb> 11.8 <sep> Crack gases <Tb> 11.9 <sep> Crack gas line <Tb> 12 <sep> Sludge entry <Tb> 12.1 <sep> Sludge <Tb> 12.2 <sep> pressure line <Tb> 12.3 <sep> shutoff <Tb> 12.4 <sep> slurry pump <Tb> 12.4.1 <sep> entry zone <Tb> 12.5 <sep> melting zone <Tb> 12.5.1 <sep> melting <Tb> 12.6 <sep> cracking zone <Tb> 12.6.1 <sep> cracking <Tb> 12.7 <sep> drying zone <Tb> 12.8 <sep> Level <tb> 12.8.1 <sep> Upper level <tb> 12.8.2 <sep> Lower level <Tb> 12.9 <sep> reactor contents <tb> 12.9.1 <sep> Wet household waste fraction <tb> 12.9.2 <sep> Melting zone Domestic waste fraction <tb> 12.9.3 <sep> Coke and liquid <tb> 12.9.4 <sep> Dried household waste <Tb> 10.12 <sep> compression zone <Tb> 12.10.1 <sep> compaction <tb> 12.11 <sep> Zone without conveying element <Tb> 12.12 <sep> screw press <Tb> 12.13 <sep> Drive <Tb> 12.14 <sep> material flow direction <Tb> 12.15 <sep> grafting <Tb> 12.16 <sep> Gases <Tb> 12.16.1 <sep> gas bubbles <Tb> 12.16.2 <sep> mixing <Tb> 12.17 <sep> spiral conveyor <Tb> 12.18 <sep> filling pipe <Tb> 12.19 <sep> Gate Valve <Tb> 12.20 <sep> slide plate <Tb> 12.21 <sep> key drive <Tb> 12.22 <sep> Level difference <Tb> 12.23 <sep> load cell <Tb> 12.24 <sep> differential pressure <Tb> 12.25 <sep> control signal <Tb> 12.26 <sep> Naphtha <Tb> 13 <sep> fuel gas cooler <tb> 13.1 <sep> Cooled fuel gases <Tb> 13.2 <sep> light liquid <Tb> 13.2.1 <sep> Thinner <Tb> 13.2.2 <sep> Fuel <Tb> 13.3 <sep> light liquid container <Tb> 13.4 <sep> light liquid feed <Tb> 13.5 <sep> feed pump <Tb> 14 <sep> mixer <Tb> 14.1 <sep> mixing vessel <Tb> 14.2 <sep> Drive <Tb> 14.3 <sep> twin shaft mixer <Tb> 14.4 <sep> circulation material <tb> 14.4.1 <sep> Warm goods in circulation <Tb> 14.5 <sep> feed pump <Tb> 14.6 <sep> Heat Exchanger <Tb> 14.7 <sep> heating medium <Tb> 14.8 <sep> mix <Tb> 14.9 <sep> entry pump <Tb> 14.10 <sep> Mischguteintrag <tb> 14.11 <sep> Viscosity and temperature control <Tb> 15 <sep> Oil Sands <Tb> 15.1 <sep> roll crusher <Tb> 15.2 <sep> fine sand <tb> 15.3 <sep> Wet sand mixture <tb> 15.4 <sep> Cold sand mixture <tb> 15.5 <sep> Warm sand mixture <tb> 15.6 <sep> Hot sand <Tb> 15.6.1 <sep> remixing <tb> 15.7 <sep> Dehumidified sand <tb> 15.8 <sep> Cool sand <Tb> 15.9 <sep> backfill <Tb> 15.10 <sep> distributor <Tb> 15.11 <sep> heat exchanger tubes <Tb> 15.12 <sep> trickle <Tb> 15:13 <sep> discharge <tb> 15.14 <sep> Heating medium circulating pump <tb> 15.15 <sep> Heating medium flow <tb> 15.16 <sep> Heating medium return <Tb> 15:17 <sep> hydrocarbon mixture <Tb> 16 <sep> PET recycling plant <tb> 16⋅n <sep> Several PET recovery plants <Tb> 16.1 <sep> PET powder <Tb> 16.1.1 <sep> PET powder discharge <Tb> 16.2 <sep> Drive <Tb> 16.3 <sep> auger <Tb> 16.4 <sep> Center pipe <Tb> 16.5 <sep> screw spiral <Tb> 16.6 <sep> conveying direction <Tb> 16.7 <sep> direction of rotation <Tb> 16.8 <sep> cooling pipe <Tb> 16.8.1 <sep> constriction <Tb> 16.9 <sep> jacketed <Tb> 16.10 <sep> coolant <Tb> 16.11 <sep> Flow direction <Tb> 16.12 <sep> cooling medium input <Tb> 16:13 <sep> cooling medium output <Tb> 16:14 <sep> hot gas supply <Tb> 16:15 <sep> hot gas outlet <Tb> 16:16 <sep> cyclone <Tb> 16:17 <sep> sluice <tb> 16.18 <sep> Lower gas velocity <tb> 16.19 <sep> High gas velocity <Tb> 16:20 <sep> section <tb> 16.21 <sep> reactor cross section <tb> 16.22 <sep> Reduced cross section <tb> 16.23 <sep> Enlarged cross-section <tb> 16.24 <sep> Annular gap cross section <Tb> 16:25 <sep> hot gas velocity <Tb> 17 <sep> evaporation device <Tb> 17.1 <sep> inner cone <Tb> 17.2 <sep> outer cone <Tb> 17.3 <sep> Plate Heating <Tb> 17.4 <sep> heating surface <Tb> 17.5 <sep> heating jacket <Tb> 17.7 <sep> cone angle <Tb> 17.8 <sep> screw screw <Tb> 17.9 <sep> Material pressure zone <Tb> 17.10 <sep> surface pressure <Tb> 17.11 <sep> melting zone <Tb> 17.12 <sep> evaporation zone <Tb> 17:13 <sep> guide casing <Tb> 17:14 <sep> rotary distributor <Tb> 17:15 <sep> Eintragsgut <Tb> 17:16 <sep> Entgasungkanäle <Tb> 17:17 <sep> radiant heat <Tb> 17:18 <sep> vent <Tb> 17:19 <sep> Schlackenaustrag <Tb> 18 <sep> separation plant <Tb> 18.1 <sep> paraffin <Tb> 18.1.1 <sep> Parafinfraktion <Tb> 18.2 <sep> feed pump <Tb> 18.3 <sep> pressure line <Tb> 18.4 <sep> scrubber <Tb> 18.5 <sep> container <Tb> 18.6 <sep> Package <Tb> 18.7 <sep> washing liquid <Tb> 18.8 <sep> Circulation <Tb> 18.9 <sep> sprayer <Tb> 18.10 <sep> dosing <Tb> 18.11 <sep> PH control <Tb> 18.12 <sep> Condensate <Tb> 18:13 <sep> horizontal conveyor <Tb> 18:14 <sep> Vertical Conveyor <Tb> 18:15 <sep> gas line <Tb> 18:16 <sep> Spiral Conveyor <tb> 18.17 <sep> Cooled circulating fluid <Tb> 18:18 <sep> supernatant liquid <tb> 18.18.1 <sep> Water vapor and gas fraction <Tb> 18:19 <sep> light liquid separation unit <Tb> 18:20 <sep> light liquid <Tb> 18.20.1 <sep> light liquid phase <Tb> 18:21 <sep> Water <Tb> 18.21.1 <sep> water phase <Tb> 19 <sep> dryer <Tb> 19.1 <sep> water vapor <Tb> 19.2 <sep> melting reactor feed <Tb> 19.3 <sep> exhaust air treatment <Tb> 19.4 <sep> exhaust <Tb> 19.5 <sep> Condensate

Claims (65)

1. Process for the treatment of highly stressed organic substances with the steps: - Enter the mixtures (3.16.2) in a reactor (3). - Melting (12.5.1) and cracking (12.6.1) under vacuum (7.2.1). - drying (3.9.1) and discharge of residues (5.9.1). - Condensation of the gaseous phase resulting from cracking (12.6.1) to liquid fuels (7.6). - Save the resulting fuels (7.6). 2. The method according to claim 1, characterized in that the material entry (1), the melting (12.5.1) and cracking (12.6.1) and the drying (3.9.1) of the residues (5.9.1) in a reactor space ( 3.21). 3. The method according to claims 1 and 2, wherein the cracking (12.6.1) in the cracking zone (12.6) of the reactor (3) and the discharge of the superheated steam (7.1) under a vacuum (7.2.1) of greater -0.6 bar occurs. 4. The method according to claim 2, wherein in a reactor (3) encompassing the heating jacket (6.1), the heating medium (6.2) flows in countercurrent (6.7) to the main flow direction (3.13). 5. The method according to claims 2 and 3, wherein from lignin-containing mixtures (3.16.1), fuels (13.2.2) in the form of wood oil (3.14.1), fuel gases (7.1.4) and coke (5.15) are obtained. 6. The method according to claims 2 and 3, wherein from solid plastic mixtures (3.15) of fossil origin, liquid fuels (7.6) are obtained. 7. The method according to claims 2 and 3, wherein from oil sands (15) and oily sludge (12.1), liquid fuels (7.6) are generated. 8. The method according to claims 5, 6 and 7 wherein by determining the chain length of the C molecules in the condenser (11), naphtha (12.26) is obtained, from which again unmixed plastics are produced in further process steps. 9. The method according to claims 2 and 3, wherein from mechanically treated household waste (3.16), liquid fuels (7.6) are obtained. 10. The method according to claims 3 to 9, wherein in addition to liquid fuels and secondary fuels in the form of fuel gas (7.13), light liquid (13.2) and coke (5.15) are obtained. 11. The method according to claims 9 and 10, wherein in the same reactor (3) simultaneously from the plastic mixtures (3.15), liquid fuels (7.6) and from the remaining organic fraction, pyrolysis (5.15.1) is obtained. 12. The method according to claim 10, wherein the secondary fuels are used to generate the process energy. 13. The method according to claims 9 and 10, wherein from the pyrolysis (5.15.1), methanol (5.19) is produced. 14. The method according to claims 9 to 13, wherein from mechanically treated household waste (3.16), introduced into a cascaded reactor (3), consisting of the functions, drying (19), melting (12.5.1) and cracking (12.6.1 ) and therefrom as end product, fuels (7.6), pyrolysis coke (5.15.1), metal (5.16) and inert materials (5.17). 15. The method according to claim 2, wherein the superheated steam (7.1) from the reactor (3) by a liquid jet pump (7.2) sucked under vacuum (7.2.1) and cooled by the cooled blowing agent (7.11) and liquid fuel (7.6 ) and fuel gases (7.1.4) are condensed. 16. The method according to claim 15, wherein the propellant fluid (7.3) for driving the liquid jet pump (7.2) from the condensed fuels (7.6), which in the circuit via a cooler (7.8) of the liquid jet pump (7.2) as cooled propellant (7.11) is supplied. 17. The method according to claims 15 and 16, wherein accelerated by the generated vacuum (7.2.1) degassing in the reactor (3) and in the material bed (3.19) and thereby secondary reactions are avoided. 18. The method according to claim 7, wherein the entry of tough oily sand and sludge (12.1), a part of the self-produced light liquid (13.2) as a thinner (13.2.1) is added. 19. The method according to any one of the preceding claims, wherein to increase the flowability, the entry material, consisting of sludge (12.1) and oil sand (15), via a mixing device (14) is heated. 20. The method according to claims 18 and 19, characterized in that are used in the thermal extraction of oil sand (15), no solvents on the basis of water. 21. The method according to claim 2, wherein the material entry into the reactor (3) diametrically opposite the gas dome (3.12) and the discharge of residues (5.9.1). 22. The method according to claim 21, wherein the reactor (3) in any inclination (3.18) is carried out, wherein the material entry (1) always takes place at the lowest point. 23. The method according to claims 1 to 7, wherein the length of the reactor in the main flow direction (3.13) in an entry zone (12.4.1) and compression zone (12.10), a melting zone (12.5) and cracking zone (12.6), and a drying zone ( 12.7) for the solid residues (5.9.1) is divided and withdrawn at the end of the overheated steam (7.1) via a gas dome (3.12) under vacuum (7.2.1) and the solid residues (5.9.1) in the form of dried hotter Slag (5.12) be discharged via a discharge lock (5.6). 24. The method according to claim 23, wherein a plurality of reactors (3 and 3⋅n) are arranged parallel next to each other and have a common feed chute (3.1) and an opposite discharge chute (5.9) and gas dome (3.12). 25. The method according to claims 22, 23 and 25, characterized in that in cascaded cascaded reactors (3) each have a common feed chute (3.1) and a common opposite discharge chute (5.9) and gas dome (3.12). 26. The method according to claims 22, 23 and 24, characterized in that in cascaded cascaded reactors (3⋅n) each reactor (3) has its own degassing device in the form of a gas dome (3.12). 27. The method according to claims 25 and 26, wherein the loading of feedstock (1.5) on the level difference (12.22) in the evaporation reactor (3.1.2) is controlled. 28. The method according to claims 25 to 27, wherein the measurement of the level difference (12.22) in the entry shaft (5.5.1) between the melt reactor (3.1.1) and the evaporation reactor (3.1.2) is located. 29. The method according to claims 25 and 26, wherein the exhaust gases from the melt reactor (3.1.1) in a cooled separation plant (18), in a paraffin fraction (18.1.1) and a water vapor and gas fraction (18.18.1) are split , 30. The method according to claim 29, wherein the paraffin (18.1) fed to the evaporation reactor (3.2.1) and the steam and gases (7.1.3) are introduced into an alkaline gas scrubber (18.4). 31. The method according to claims 25, 26 and 30, wherein the supernatant liquid (18.18) from the gas scrubber (18.4) in the light liquid separation plant (18.19), in a water phase (18.21.1) and a light liquid phase (18.20.1) is separated. 32. The method according to the patent claims 4 and 5, characterized in that the mixing (12.16.2) of the reactor contents (12.9) by the gas bubble formation (12.16.1) takes place. 33. The method according to claims 2 and 3, wherein the heating of the reactor contents (12.9) via a heating medium (6.3) is based on sodium chloride. 34. The method according to claims 2, 3 and 33, wherein the heating medium (6.3) via a hot plate (6.12) with an open flame (6.10.1) is heated. 35. The method according to claims 2, 3 and 33, wherein the heating medium (6.3) encloses the inner tubes (6) of the reactor (3). 36. The method according to claims 34 and 35, wherein the heat input into the inner tubes (6) takes place indirectly, in that the open flame (6, 10, 1) first heats the heating medium (6.3) and then the heating medium (6.3) the reactor contents (12.9) heated. 37. Method according to claims 9 and 10, wherein constituents of polyethylene terephthalate (PET) introduced into the reactor (3) are introduced via the purified hot gases (10.5) at 400 ° C. and the terephthalic acid contained in a PET recovery plant (16) at 350 ° C, precipitates on the cooling wall of the cooling tube (16.8) and is discharged as a PET powder (16.1). 38. The method according to claim 37, wherein with the hot gas velocity (16.25) the cooling and Pulveraustragsvorgang is regulated. 39. The method according to claim 4, 9 and 10, wherein with a screw screw (17.8), mixtures (3.16.2) and biomass (3.14) are compressed and with a force of at least 4 kg / cm2 against a heating surface (17.4) be pressed. 40. The method according to claim 39, wherein the heating surface (17.4) is conically designed as an inner cone (17.1) or outer cone (17.2), as well as a plate heater (17.3). 41. The method according to claim 39 and 40, wherein at the opposite end of the screw screw (17.8) a degassing opening (17.18) and a slag discharge (17.19) is arranged. 42. The method according to claims 17 and 41, wherein through the selected lumpiness of the compressed mixtures (3.16.2) degassing channels (17.16) form over which by the applied vacuum (7.2.1) the superheated steam (7.1) is withdrawn. 43. The method according to claim 39, wherein the passage of mixtures of substances (3.16.2) having a melting point of less than 250 ° C, these are cooled in the guide casing (17.13). 44. The method according to claims 4, 12 and 33, wherein the self-generated fuel gases (7.13) are burned in a gas turbine (8.7) and with the hot gases (8.10) via a Heizmediumerhitzer (8.2), the process heat is generated. 45. The method according to claim 44, wherein via the gas turbine (8.7), the total required electrical energy (8.9) is generated. 46. The method according to claim 21 to 23, wherein each individual reactor (3) by a slide (12.19) is switched on or off. 47. The method according to claim 2 and 6, wherein the material entry (1) Schleissstoffe miteeinggeben as Umlaufgut (1.4), with which the caking and deposits on the heating surfaces on the inner tube (6) are cleaned. 48. The method according to claim 47, wherein during the material discharge the circulating material (1.4) is screened off and added again to the material entry (1). 49. Apparatus for carrying out the method according to claims 40 to 42, in that the heating surface arrangement is designed as a plate heater (17.3) or as an inner cone (17.1) or outer cone (17.2). 50. Apparatus for carrying out the method according to claim 49, wherein the heating surface arrangement consists of a combination of inner cone (17.1) and outer cone (17.2), as well as a flat plate heater (17.3). 51. A device for carrying out the method according to claims 37 and 38, by with rotating screw helix (16.5) of the screw conveyor (16.3), the terephthalate acid powder, known as PET powder (16.1) scraped from the surface of the cooling tube (16.8) and the cyclone separator (16.16). 52. Apparatus for carrying out the method according to claims 38 and 51 by the low gas velocity (16.18) and the high gas velocity (16.19) is adjusted over the annular gap cross section (16.24) from the screw conveyor (16.3) and the cross section of the cooling tube (16.8). 53. Apparatus for carrying out the method according to claim 21, 22 and 23, by the material transport in the reactor (3) by a conveyor in the form of a conveyor spiral (4), which extends over the entire heated effective length of the reactor (3) and via a Geared motor (4.1) is driven. 54. Apparatus for carrying out the method according to claim 53, in that on the entry side of the reactor (3) the press screw (12.12) is provided with its own drive (12.13). 55. Apparatus for carrying out the method according to claim 53 and 54, in that a gate valve (12.9) is located between the press screw (12.12) and the conveyor spiral (4). 56. An apparatus for carrying out the method according to claim 33, by by cyclically changing the direction of rotation of the conveyor spiral (4), the residence time of the reactor contents (12.9) in the reactor (3) is extended and introduced shear forces, which promote the mixing (12.16.2) and fresh material leads to the enamel surfaces of the inner tube (6). 57. Apparatus for carrying out the method according to claim 23 and 53, by drying in the drying zone (12.7) the inert residues (5.9.1) and non-cracked carbon residues through the heated inner tube (6) and through the delivery spiral (4) as coke, Metal and inert materials (5.12.1) promoted in the discharge chute (5.5), and in the drying zone (12.7) cleans the heating walls of deposits and caking. 58. Apparatus for carrying out the method according to claim 21 and 22, by determining with the adjustable inclination (3.18) of the reactor (3), the backmixing (15.6.1) of the reactor contents (12.9). 59. Apparatus for carrying out the method according to claim 23 and 53, by the conveyor spiral (4) over the entire length of the reactor (3), coke, metal and inert substances (5.12.1), are conveyed to the discharge shaft (5.5). 60. Apparatus for carrying out the method according to claim 53, wherein the dry residues (5.9.1) are cooled in a discharge lock (5.6) with a refrigerant in the form of liquid nitrogen (5.11). 61. Apparatus for carrying out the method according to claim 7 and 35, by the hot sand (15.6) in a trickle bed reactor (15.12), is cooled by removing heat. 62. Apparatus for carrying out the method according to claim 61, wherein the extracted heat via a heating medium circuit (15.15 and 15.16) of the heating of the oil level (15) is supplied. 63. Apparatus for carrying out the method according to claim 2 and 51, by pressing with the press screw (12.12) the fresh material (3.16.1) to a gas-tight plug (12.15) is pressed. 64. Apparatus for carrying out the method according to claim 53 and 63, by the plug (12.15) removed on the opposite side by the conveyor spiral (4) and in the melt reactor (3.1.1) and evaporation reactor (3.1.2) is promoted. 65. Apparatus for carrying out the method according to claim 59, wherein the conveyor spiral (4) without centering, loosely in the inner tube (6) and via a drive shaft (4.11) with a star coupling consisting of a drive star (4.12) and a driven star (4.13) is moved.