CH703614A2 - A continuous process and apparatus for melting of lignocellulosic biomass to wood oil or waste plastics and petroleum-containing sludge and household waste to fuel gases and liquid fuels. - Google Patents

Abstract

Disclosed is a method in which lignocellulosic biomass liquefied in the same device to wood oil or treated polluted plastics and organic liquids and sludge and oil sands and pretreated household waste to liquid hydrocarbons and fuel gases and inorganic residues and pollutants are removed as slag.

Description

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

With the ablative flash pyrolysis presented here, can be melted and vaporized in one and the same reactor system in separate streams of lignocellulosic biomass, mixed plastics, and petroleum-containing sludges and sands by heating at hot contact surfaces under oxygen exclusion.

In contrast to the so-called hot pyrolysis or gasification, which takes place by selective oxygen input 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 and is then condensed and discharged at the lignocellulosic biomass as a pyrolysis oil and fuel gases.

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

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-containing materials wood oil, fuel gases and coke is obtained. The fuel gases and coke are used to generate the process energy and the fuel 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, this 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.

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), as well as processed household waste (3.16) for the production of fuel oil (7.1 ), Fuel gases (7.13) and coke (5.9).

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 arranged side by side.

After the filling of the lock (2), the content is purged 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) through the material distribution (3.5) alternately in the direction of A and B.

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

By the contact of the biomass (3.14), as well as the processed household waste (3.16) with the hot surface of the inner tube (6), the biomass (3.14) and household waste (3.16) is melted under oxygen exclusion and vacuum at the hot contact surface , The resulting liquid film evaporates immediately and leaves as superheated steam (7.1), with a temperature between 450 to 500 ° 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 processed household waste (3.16) is compressed and pressed against the hot wall of the inner tube (6) and thereby the Abschmelzvorgang is accelerated.

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 460 ° to 520 ° C, is sucked by the liquid jet pump (7.2), which also generates the vacuum 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 1m3 to about 4 liters. This process creates and holds the vacuum. By applying vacuum in the reactor (3), secondary reactions in the gas stream are avoided in order to avoid quality losses in the pyrolysis oil.

With a system for refrigeration (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 fuel gases (7.13) 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).

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 treated household waste (3.16), for the production of fuel oil (7.1), Fuel gases (7.13) and slag (4.6).

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 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) by means of 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 the 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 processed 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) is melted under oxygen exclusion and vacuum 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 the 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, the long-chain hydrocarbons condense (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 are recycled via the sluice (11.4) to the reactor (3) for re-cracking.

Fig. 3 shows a longitudinal section through the 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 product (3.16.1) is pressed through the material distributor (3.2) in the conveying spirals (4) of the melting tubes (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 conveyor spiral by reversing the direction of rotation (4.3), 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 better mixing of the melt (4.8) takes place and the contact surfaces on the heated inner tube (6) by the rotational movement, the spiral (4) of caking, carbon deposits and contaminants is cleaned and thus an optimal heat input ( 6.6) in the melt (3.17) guaranteed.

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 the discharge conveyor (5) and discharge lock (5.6) from the reactor (3) as dry material in the form of cold Slag (5.13) is discharged.

Figure 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 melt tubes (4.7). Shown are five pieces of parallel arranged melting tubes (4.7), 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 oily sand.

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).

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.

The length of the reactor (3) is divided into three 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 portions of the sludge (12.1) are melted by the action of temperature to a honey-like mass. In the cracking zone (12.6) is evaporated by the higher temperature between 380 ° C to 420 ° C, the reactor contents (12.9) 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 effect of temperature, the long-chain carbon molecules 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) are 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 molecules.

The residence time of the reactor contents (12.9) depends on the material composition of the fed sludge (12.1). In particular, low-boiling material is introduced which shortens the residence time in the reactor (3) and thus can increase the throughput of sludge (12.1). 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 (5.12) simultaneously fulfills the function of a vacuum-tight discharge sluice.

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

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.

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 mixing system.

In the event that tarry and schweröihaltige 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.

About the viscosity and temperature control (14.11), the supply of heat via the heat exchanger (14.6) and thinner (13.21) via the feed pump (13.5) is controlled. In this case, feed pumps (13.5) are used, which are used to convey concrete.

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

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 to Cracking temperature between 350 ° C to 480 ° 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.

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), not shown here with floats, which act on the density system, the water level is detected and discharged via 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 with a conveyor, here shown as a feed pump (13.5) as a thinner (13.2.1) of the mixing device (14). The excess of light liquid (13.2) is used as fuel (13.2.2) for process heating or other purposes.

If there is a defect or when starting up the process, it must be added from external sources, light liquid (13.2) on the light liquid feed (13.4). 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, relating to the condensation plant (7) and the fuel gas cooler ( 13), the production of the light liquid (13.2) closes the dilution cycle.

Fig. 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 circulating 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 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 passed 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), get into the liquid jet pump (7.2) and are there abruptly cooled by the Treibfiüssigkeit (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 water extraction control (7.16 and 7.17) with the drainage 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 fed to the fuel gas cooler (13) 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) must be supplied in the form of kerosene or gasoline.

FIG. 12 shows the treatment apparatus and method steps in the case of a cascaded arrangement of the reactors (3.1.1 and 3). This arrangement is used and in the material entry (1) of abrasive mixtures in the treatment of auto shredder light fractions.

In the series connection of the first reactor is operated as a preheating 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 reactor (3). 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) have the same inclination (3.18 and the level (12.8).) The level (12.8) also limits the cracking zone (12.6) in the reactor (3) ), the supernatant and the slag (4.7) is dried by the heat input and fed through the discharge chute (5.5) of the initial spiral.

The operating temperature in the reactor is between 380 ° C to 420 ° C. The cracking gases leave as superheated steam (7.1) 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.

LIST OF REFERENCE NUMBERS

[0090] <tb> A <sep> turning and conveying direction <tb> B <sep> Rotation and conveying direction <Tb> 1 <sep> Material entry <Tb> 2 <sep> sluice <Tb> 2.1 <sep> Gate Valve <Tb> 2.2 <sep> inert gas <Tb> 3 <sep> reactor <Tb> 3.1 <sep> insertion slot <Tb> 3.1.1 <sep> preheating <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> 3.10 <sep> discharge zone <Tb> 3.11 <sep> degassing <Tb> 3.12 <sep> gas dome <Tb> 3.13 <sep> main current direction <Tb> 3.14 <sep> Biomass <Tb> 3.15 <sep> plastic mixture <tb> 3.15.1 <sep> Autoshredder light fraction <tb> 3.16 <sep> Recycled household waste <Tb> 3.16.1 <sep> fresh material <Tb> 3.17 <sep> melting <Tb> 3.18 <sep> inclination <Tb> 3.19 <sep> material fill <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> 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> 5.10 <sep> slag cooler <Tb> 5.11 <sep> Liquid Nitrogen <tb> 5.12 <sep> Hot slag <tb> 5.13 <sep> Cold slag <Tb> 6 <sep> inner tube <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> 6.7 <sep> countercurrent <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> 7.2 <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> Products Oil <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> Products oil drain <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> 8 <sep> heat generation <Tb> 8.1 <sep> multifuel <Tb> 8.2 <sep> Heizmediumerhitzer <Tb> 8.3 <sep> Circulation <Tb> 8.4 <sep> exhaust stack <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> Füllkörperverpackung <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> 11.8 <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> 12.5 <sep> melting zone <Tb> 12.6 <sep> cracking zone <Tb> 12.7 <sep> drying zone <Tb> 12.8 <sep> Level <Tb> 12.9 <sep> reactor contents <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> Leichtflüssigketiszuführung <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

Claims (25)

1. Process for the treatment of highly stressed organic substances with the steps: - Enter the substances in a reactor. - Melting and cracking and discharge of slags. - Condensation by cooling the resulting after cracking gaseous phase to combustible light liquid. - Save the resulting light liquid. 2. The method according to claim 1, characterized in that the melting and cracking and drying of the organic residues takes place in a reactor space. 3. The method according to claim 2, wherein in a heating jacket encompassing the reactor, the heating medium flows in countercurrent to the material flow. 4. The method according to claims 2 and 3, wherein from lignin-containing mixtures, fuels in the form of fuel oil, fuel gases and coke are obtained. 5. The method according to claims 2 and 3, wherein from solid plastic mixtures of fossil origin, liquid fuels are obtained. 6. The method according to claims 2 and 3, wherein from petroleum-containing sand and sludge mixtures, liquid fuels are produced. 7. The method according to claims 5 and 6, wherein by determining the chain length of the C molecules in the partial condenser, naphtha is recovered, from which again unmixed plastics are produced in further process steps. 8. The method according to claims 2 and 3, wherein from mechanically treated and freed from impurities household waste, liquid fuels are obtained. 9. The method according to claims 4 to 8, wherein in addition to liquid plastics and secondary fuels in the form of gases, light liquid and coke are obtained. 10. The method according to claim 9, wherein the secondary fuels are used to generate the process energy. 11. The method according to claim 2, wherein the cracking gases are sucked from the reactor by a liquid jet pump under vacuum and cooled by the cooled liquid jet and condensed to liquid fuel and fuel gases. 12. The method according to claim 11, wherein the liquid jet for driving the vacuum pump from the condensed liquid fuels, which is supplied in the circuit via a cooler of the liquid jet pump as a blowing agent. 13. The method according to claims 11 and 12, wherein accelerated by the vacuum generated the degassing in the reactor and in the material bed and thereby secondary reactions are avoided. 14. The method according to claim 6, wherein the entry of tough oily sludges, a part of the self-produced light liquid is added as a circulating diluent. 15. The method according to any one of the preceding claims, wherein to increase the flowability, the entry material is heated via a heat exchanger device. 16. The method according to claims 14 and 15, characterized in that are used in the thermal extrusion of oil sand, no solvents on the basis of water. 17. The method according to claim 2, wherein the material input into the reactor diametrically opposite the Crackgasaustrag and the solids discharge. 18. The method according to claim 17, wherein the reactor is designed in any position from horizontal to vertical, wherein the material entry always takes place at the lowest point. 19. The method according to claims 1 to 6, wherein the length of the reactor in the material flow direction in an entry zone, a melting zone, a cracking zone, and a drying zone for the solid residues is divided and withdrawn at the discharge end the cracking gases through a gas dome and the solid residues in Form of slag to be discharged through a lock. 20. The method of claim 19, wherein a plurality of reactors are arranged in parallel side by side and have a common entry and an opposite discharge and degassing. 21. The method according to claims 18, 19 and 20, characterized in that in cascaded one behind the other reactors each has a common entry device and opposite discharge and degassing. 22. An apparatus for carrying out the method according to claim 17, 18 and 19, by the material transport in the reactor by a conveyor in the form of a spiral, which extends over the entire effective length of the reactor and is driven by a geared motor. 23. The method according to claims 19, 20 and 21, characterized in that in cascaded one behind the other reactors each reactor has its own degassing. 24. An apparatus for carrying out the method according to claim 22, by changing the direction of rotation of the transport spiral by cyclic change, the residence time of the reactor contents in the reactor is extended and introduced shear forces which promote the mixing and supplies fresh material to the melt surfaces. 25. Apparatus for carrying out the method according to claim 22 and 23, by drying in the drying zone, the inert residues and non-cracked carbon residues through the Heizwandung and promoted by the transport spiral as slag and coke in the discharge chute, and cleans the heating walls of deposits and caking.