CH706804A2 - Melting and evaporating lignin-, cellulose-, and carbonaceous material streams, comprises forming closed and interconnected unit with e.g. drier, filling device, pyrolysis reactor and discharging of the solids using hot gases and wet steam - Google Patents

Abstract

Melting and evaporating lignin-, cellulose-, and/or carbonaceous material streams, comprises forming a closed and interconnected unit with a drier, a filling device, a pyrolysis reactor and conducting heat and electricity together with material flow in moderately energetic manner introducing the combustion gases through a wet product-inlet, and discharging of the solids using hot gases and the wet steam. An independent claim is also included for a device for carrying out the above mentioned method, where material transport takes place in the reactor by a conveyor from screw paddle, which extends over the entire pitch length of the heated evaporation reactor.

Description

The invention relates to a method for melting and evaporating lignin, cellulose, and carbonaceous streams or mixtures thereof, by inductive heating with homogeneous substance-free mixtures and contaminated, provided with impurities mixtures, the heat input via tube heat exchanger by liquid heat transfer medium, wherein the dryer, the filling device, the pyrolysis reactor and the heat generation together, stoffstrommässig and energetically form a closed and interconnected unit and produce as products, fuel gases to cover the process energy, and as products, liquid fuels and coke, slag or charcoal.

In the course of crude oil and energy and the increasingly restrictive requirements of the authorities with regard to the treatment of waste and the recycling of recyclables, there is great interest in the treatment of plastic waste, which are sorted out, for example, from the residual waste and the conversion of young people Raw materials in storable and transportable liquid energy.

From WO 2005/071 043 A1 and WO 2008/022 790 A2 a treatment process is known in which plastics are processed in a continuous process to oil.

The previously cleaned and sorted plastic materials are first compressed under exclusion of air and fed to a melting vessel. In this, a separation into a first liquid phase, a first gas phase and a residue fraction takes place. The liquid phase and the first gas phase are fed to an evaporator in which a second liquid phase and a second gas phase are formed. The second liquid phase is further heated in a reheater. The resulting third gas phase is fed together with the second gas phase from the evaporation vessel to a cracking tower in which long-chain hydrocarbons are cracked. The resulting gas is then condensed in a condenser to give light weight.

This complex process management with Aufschmelzbehälter, several evaporation or reheating stages and a cracking plant and capacitors requires considerable device complexity.

From WO 2008/022 790 A2 also a multi-stage continuous process is presented with which clean and freed from impurities mixed plastics are processed into oil by the plastics are compressed under exclusion of air and fed to a first reflow stage and a downstream loop reactor, the sturgeon - And sediment are removed at the bottom point as wet mass.

The loop reactor is designed as a cracking reactor and the cracking gases produced are processed in a multi-stage condensation plant to fuel gases and liquid fuels.

Further processes for the thermocatalytic depolymerization of waste plastics can be found in the following patents: - WO 2005/087 897 A1, Ozmotech Pty Ltd, Notting Hill, Victoria 3168 (AU) - EP 2 161 299 A1, Handerek, Adam, 43-300 Bielsko-Biala (PL) - WO 2005/078 049 Al, Torkarz, PL-97-400 Belchatow (PL)

WO 97/06 886 shows a sand-bed reactor in which finely ground biomass is mixed with hot sand and thus degraded by pyrolysis. The treatment and decomposition of the biomass into small solid particles with grain <1.5 mm is very energy-consuming and reduces the efficiency of the process.

Further methods for pyrolysis of biomass can be found in the following patents and publications: - WO 03/057 800, Bridgewater, Peacoke - WO 2006/117 006, Bech, Dam-Johansen

In the field of flash pyrolysis biomass is pyrolysed under hot conditions within one second on hot surfaces, decomposed at temperatures around 500 to 600 ° C and in gaseous, liquid and solid starting materials.

From WO 2004/076 591 a treatment process is shown in which pressed over a plurality of revolver-like pressing tools, compressed biomass is pressed against a rotating heating plate and evaporated. This complex, multi-stage charging via plunger against a rotating hotplate requires considerable device complexity.

Compared to the listed methods, the invention has for its object to provide methods and devices with which organic material streams can be treated with minimal technical equipment effort to recoverable energy.

In homogeneous impurity mixtures according to the invention the entry of dried renewable raw materials, olives and marc or mechanically pretreated household waste or fractions thereof, via an extruder with which the density of about 1.2 kg / dm <3> and the dimensionally stable and rotating takes place Pressing a strand against a fixed hot plate with a force of 1200 to 1500 kg / cm <2>.

The heat supply to the heating plate to the contact surface of the material to be melted must be done faster than the heat extraction is derived by the melting process. The temperature of the hot plate can be adjusted depending on the material composition and the contact pressure, in a range of 300 ° C to 800 ° C, while the heat output is between 80 watts per second to 200 watts per second.

The pulsation of the extruder between 1 to 4 cm per second, is compensated by the suspension and the adjustable back pressure of the hot plate. The cleaning of caking and inorganic residues on the heating plate is carried out by the introduction of shear forces on the rotation of the press strand. The solid residues in the form of inert material, organic slag and coke or charcoal are discharged as dry matter over the exhaust shaft with gas-tight lock from the pyrolysis reactor.

The hot gas or cracking gas leaves the pyrolysis reactor under vacuum over the gas dome and passes through the fine dust in the downstream condensation stages. In the first condensation stage, the vacuum is set between -5 mbar to -200 mbar via a liquid jet pump.

By the vacuum and the rapid cooling and deposition of the products secondary reactions are avoided, which would lead to yield and quality losses of pyrolysis.

The entire process duration of the pressing of the extrudate on the hot plate, the melting and evaporation, the condensation and cooling to the products takes in the presented here flash pyrolysis a maximum of 2 seconds.

In the pyrolysis of dried sludges such as sewage sludge and oil tanker sludge with high sand content and lumpy material such as autoshredder light fraction with high impurity and metal content, a screw press is used as a volumetric conveyor with low back pressure. With the weak pressure build-up, atmospheric oxygen is squeezed out and abrasions in the compression area are avoided.

The loosened compressed strand is entered in the lower third of the oblique monotube pyrolysis. The throughput time from entry to evaporation and discharge of the dry inert materials, metals and slags refers to the input material composition and is 3 to 6 hours.

With a heated screw pump, the liquefied substrate is withdrawn as a partial stream in the middle of the Einrohrpyrolysereaktors and registered at the lowest point of the Einrohrpyrolysereaktors again.

By this recirculation of the hot melt (19.20), the cold input material is melted immediately, with the mixing ratio between the cold input material and the Reziklat is 1:10.

The monotube pyrolysis reactor has a heating jacket enclosing the pyrolysis reactor in that a pressureless heating medium flows countercurrently to the material flow and advantageously consists of molten salt or thermal oil.

The temperature range in the single-tube pyrolysis reactor refers to the input material composition and is over the entire length, adjustable between +300 ° C to +425 ° C. As stirring and transport means a screw shovel, consisting of a spiral with at least 3 pieces. Through continuous airfoils, which ensure at high temperatures that the spiral does not deform and at the same time the reactor contents thoroughly mixed by the change of direction.

In single-tube pyrolysis find, starting with the entry of the press strand in a row, the operations: mixing, melting, evaporation and discharge of the dried residues such as inert materials, slag, coke or charcoal instead. In this case, the drive of the screw shovel is at the upper end of the inclined monotube pyrolysis reactor and above the maximum fill level.

The discharge of the dried and hot residues is carried out by the spiral of the screw shovel in the discharge chute and a gas-tight lock in the slag cooler. Opposite the discharge shaft is at the upper end of the gas dome over which under vacuum, the hot gases or cracking gases are drawn from the monotube pyrolysis reactor. And get over the particulate matter in the downstream condensation stages in which a liquid jet pump, the vacuum between -5 mbar to -200 mbar is set.

Fig. 1 shows the structure of the ablative flash pyrolysis for melting and evaporation of lignin, cellulose, and carbonaceous streams (3.15) or mixtures thereof by the dried material stream (3.15) in the extruder (3.7) compacted and the extrudate (3.8) is pressed against the stationary heating plate (18.6) with the completion of oxygen via the rotating orifice (3.36 and 3.37) and the organic material contained in the extrudate is evaporated and the resulting hot gases (3.21) are conveyed via the gas dome (3.19) under a defined vacuum (3.19). 18.12). The material-specific negative pressure is between -5 to -200 mbar.

Above the withdrawal shaft (3.20), the inert solids (3.22), the slag (3.23) and in the evaporation of lignin-containing material streams (3.15) leave the charcoal (3.24) the pyrolysis reactor (3).

By regulating the following three parameters: 1) Material composition of the material stream (3.14) 2) the contact pressure (3.14) and associated material density 3) The temperature of the surface (18.6.1) of the heating plate with energy input via the induction coil (18.5) the desired amount of energy production in the form of liquid fuels (14.2), fuel gases (15.1) and the accumulation of solids (3.22) such as slag (3.23) and charcoal (3.24) is set, depending on the material composition of the contact pressure (3.14) between 1200 to 1500 kg / cm <2> and the surface (18.6.1) of the heating plate (18.6) has a temperature between 400 ° C to 1200 ° C, the material density of the pressed strand (3.8) at least 1.2 kg / dm <3> is and the energy input in the material flow between 100 to 1200 watts times second.

When material heaps (3.30) with thermoplastic properties of the extrudate (3.8) which is heated by the frictional heat in the cone (3.34) is cooled over the cooling jacket (3.3) in order to ensure the shape and pressure stability.

The arrangement of the cooling jacket (3.3) can be arranged in front of or behind the cone (3.34), or on both sides.

The excitation of the induction coil (18.5) is carried out by the induction generator (18.10) via the terminals energy input (18.10.1) and energy output (18.10.2).

The cooling of the induction generator (18.10) via the cooling water center (17) with the compounds, cooling water inlet (18.11.1) and cooling water outlet (18.11.2)

In the dryer (1), the moist material bed (1.6) in conjunction with the CHP plant (16) by the hot exhaust gases (16.5) dried. In Figs. 7 and 8, the material flow and energy network is shown and described in detail.

In the direct firing of heat generation (4) with the fuel gases (4.1) drying with the dry exhaust gases (1.7) generated by the burner (4.2). FIGS. 11 and 12 show and describe the energy network in detail.

The entry port (1.2) of Nassguteintrags (1.1) is the Trockengutaustrag (1.15) diametrically opposite, the hot gas channel (1.8) for the introduction of dry exhaust gases (1.7) from the CHP plant immediately adjacent to the Trockengutaustrag (1.15) is located and the wet gas duct (1.12) with the outlet of the moist water vapor (1.11) with respect to the material flow direction (1.14) diametrically opposite the hot gas channel (1.8).

The screw shovel (1.5) is enclosed in front of a casing pipe (1.3) in which the material bed to be dried (1.6) is located, which moves by the rotational movement (A and B) of the screw shovel (1.5) in the material flow direction (1.14) and by periodically changing the direction of rotation (A and B) of the drive (1.4), based on the direction of the exhaust gas flow (1.7.1), the material bed (1.6) is moved in co-flow (1.15) or counterflow (1.16), the main material flow direction ( 1.14) with the direction of rotation (B) has the priority to promote the dry material (1.18) for Trockengutaustrag (1.17).

Section A-A shows the arrangement of the blades (1.5.1) with which the material bed (1.6) by the changing direction of rotation (A and B) constantly by the material turnover (1.6.1) new surfaces are created, which by the hot exhaust gas flow (1.7.1) are dried off.

In Figs. 9 and 10, the construction and function of the screw shovel is shown and described in detail.

The dry material (1.18) is pressed by the screw shovel (1.5) in the filling device (2), shown here as a spiral (2.4), guided in a filling tube (2.1) and a drive (2.3) with which the dry material (1.18 ) is conveyed into the filler neck (3.1) of the extruder (3.7).

2 shows a section through the pyrolysis reactor (3) and evaporation reactor (18) equipped with an electric induction heater (18.1.1), consisting of an inert mounting plate (18.4) made of granite or ceramic, an induction coil (18.5) to excite the steel heating plate (18.6).

Below the consisting of ferromagnetic material Stahlheizplatte (18.6), there is the current-carrying induction coil (18.6), which generates a magnetic alternating field. This indexes in the overlying metallic Stahlheizplatte (18.6) by the induction eddy currents and thus heat, which melt and evaporate the pressed strand (3.8). The usual frequency of the alternating field is in the range between 30 to 100 kHz.

In the lower half of the pressure layer (18.19) is shown. In the upper half of the initial or rest position (18.18) with the adjustable gap adjustment (3.17) between the mouth (3.37) and the hot plate (18.6) is shown and explains the Abschmelzvorgang of the press strand (3.8), which adjustable within 0.5 to 5.0 Seconds expires: a) The extruder (3.7) presses the extrudate (3.8) against the hot plate (18.6). With the contact pressure (3.14), the mounting plate (18.4) is pressed against the prestressed spiral spring (18.13) and shifts by the adjustable conveying path (18.3) in the feed direction (18.20) and biases the coil spring (18.13.1). b) Simultaneously with the material feed (3.15.1), the extrudate (3.8) is melted off by the action of heat of the heating plate (18.6) and evaporated to hot gases (3.21) c) By the pressure of the tensioned spiral spring (18.13.1) and the ongoing Abschmelzvorgang, shifts the mounting plate (18.4) in the reverse direction (18.21) until the end position according to the set gap adjustment (13.17) is reached again.

As an example, in Fig. 2, a tensioning device with coil spring (18.13), clamping disc (13.14) and clamping screw (18.16) for pressure adjustment (18.17) shown. Other solutions can also be used, such as controllable hydraulic or pneumatic systems.

3 shows a section through the center axis of an extruder (3.7), which presses against the mounting plate (18.4) with the press strand (3.8). The mounting plate (18.4) is equipped with the heating plate (18.6) and the associated induction coil (18.5).

The gap adjustment (3.17) between the mouth (3.37) and the heating plate (18.6), shown here as a set screw construction with a metal compensator (3.16). In this case, other automated mechanical or hydraulic devices can be used as adjusting device (3.18).

In order to effect the mutual rotational movement (3.36) of the mouth (3.37), a geared motor (3.41) with drive pinion (3.39) and ring gear (3.38) is shown as an example of a variant embodiment.

Thus, the heating plate (18.6) can not move by the rotational movement (3.36), this plate is square or as shown in section A-A formed as a polygon.

The loading of the extruder (3.7) with dry material via the filling device (2), in which the spiral (2.4) stuffs the dry material (1.13) in the press shaft (3.30.1). As a result of the lifting movement (3.33) of the piston (3.32), the material bed (3.30) is pressed against the cone (3.34) and compacted.

Fig. 4 shows a section through the mouth (3.37), which is provided with grooves (3.43), so that the compressed material flow (3.44) is rotated by the rotational movement (3.36).

5 shows the mouth (3.37), formed as a tube (3.37.1) as a square or polygonal (3.37.2) with a centrally arranged loose partition (3.42), which in a guideway (3.42.1) is held and pressed by the contact pressure (3.14) against the heating plate (18.6). This partition consists of a non-electrically conductive material, preferably of ceramic, so that it is ensured that no heating by the induction coil (18.5) can take place.

Fig. 6 shows the section B-B with the loose partition (3.42), held by the guideway (3.42.1). By the contact pressure (3.14) and the rotational movement (3.36) of the mouth (3.37) the surface (18.6.1) of the hot plate (18.6) of caking, such as solids (3.22) and Slag (3.23) and carbon build-up (3.46) constantly cleaned.

Fig. 7 shows the framed scope of the claims in the dryer (1), the filling device (2), the pyrolysis reactor (3) and the heat and power generation (4 and 16), which together, stoffstrommässig and energetically a closed and connected unit and have a wet goods entry (1.1), the entry of the fuel gases (4.1) and the discharge of the solids (3.22) of the hot gases (3.21) and the moist water vapor (1.11).

Fig. 8 shows the scope of the claims (x) and for explanation, the peripheral equipment parts, which are outside the claim and corresponding to the prior art.

The entry of moist, pumpable, organically highly loaded sludge (5) such as sewage sludge or large kitchen waste or solid solids (6) such as biomass or household waste in the dryer (1), which as drying energy with the exhaust gases (16.5) from the CHP Plant (16) is operated.

The moist water vapor (1.11) from the dryer (1) is supplied to the condenser (9) which also fulfills the function of an exhaust air scrubber and depending on the requirements of the exhaust air quality, this is passed through a biofilter (10) and blown off.

The hot gases (3.21) are pre-cooled in the partial condenser (11) and long-chain carbon compounds are precipitated out as condensates (11.3) and fed again to the evaporation process.

In the spray cooler (12) the vacuum is generated via the liquid jet pump (12.8), with which the hot gases (3.21) are sucked out of the gas dome (3.19).

With the application of the vacuum (18.12) unwanted secondary reactions, as well as the formation of paraffin in the gas stream and their deposits in pipes and wall surfaces sustainably prevented.

The condensable gases (3.21) leave the spray cooler (12) as liquid fuels (12.2) and are dewatered in the light liquid separation plant (13). The dewatered liquid fuel (12.2) is spent in the liquid fuel storage (14) for further use.

The non-condensable gases (12.9) leave the spray cooler (12) as fuel gases (15.1) and enter the gas reservoir (15). The fuel gases (15.1) are burned in the CHP plant (16) and operated with the hot exhaust gases (16.5) of the dryer (1) and generated with the mechanical energy through the generator (16.1), the electrical energy for the operation of the entire system.

The solids (3.22) from the pyrolysis reactor (3) pass through the lock (6) either in the thermal oxidation (7) or in the slag cooler (8).

In the treatment of sand-containing sludges such as sewage sludge and Öltankerschlamm the dry and heated to +525 ° C sand after pyrolysis with tar-like lumps is dirty. In thermal oxidation, the hot sand is burned with a screw shovel (1.5) and by adding technical oxygen (7.2) at temperatures above + 1200 ° C. The generated hot gases (7.5) are fed as drying energy to the dryer (1).

The slags (8.3) from the treatment of renewable raw materials, mixed plastics and waste components is supplied to the slag cooler (8) for cooling, cooled with the cooling jacket (8.4) and discharged through the lock (6). In the process, the valuable substances such as metals, carbon compounds and inert substances contained in the dry slag (8.3) are subsequently separated and sent for recovery or disposal.

FIGS. 9 and 10 show a screw shovel (1.5) which is used as a transport and circulation device in the dryer (1) and evaporation reactor (19).

On the spiral (1.5.2) placed and connected distributed on the circumference at least three pieces of blades (1.5.1) with which the material bed (1.6) by the rotational movement (A and B) raised and the material conversion (1.6. 1) in the pouring direction (1.6.2) is dropped.

The number of blades (1.5.1) depends on the diameter of the spiral (1.5.2) and the composition of the material bed and their temperature.

When using the screw shovel (1.5) in an evaporation reactor (19) in which the temperature is between + 380 ° C to 650 ° C, the profile of the blades (1.5.1) additionally fulfills the function of a static reinforcement of the spiral ( 1.5.2), which would deform or buckle at these high temperatures.

11 shows an evaporation reactor (19) which is filled via the upstream dryer (1), the filling device (2) and the extruder (3.7) with dry material (1.13). By compressing the extruder (3.7) it is ensured that no atmospheric oxygen together with the extrudate (3.8) in the reactor space (19.1.1) is miteingetragen.

The inclination (19.8) of the evaporation reactor (19) depends on the composition of the material bed (1.6) When vaporizing material flows containing abrasive material, such as sewage sludge, oil tanker sludge and household waste or fractions thereof, the inclination (19.6) is between 3 and 8 degrees , For plastic fractions, the inclination is set to greater than 10 degrees.

The loading of fresh material in the reactor space (19.1.1) always takes place at the lower end of the inclined evaporation reactor (19) and the withdrawal of the hot gases (3.2.1) and the solids (3.22) takes place at the upper end.

The drive for the screw shovel (1.5) with the drive shaft passage (1.4.1) and the shaft seal (1.4.2) is always located at the upper end of the evaporation reactor (9) and thus outside contact with the reactor contents (19.8).

In the same reactor space (19.1.1) is carried out under vacuum (18.12) the material with dry material (1.13) the melting and evaporation in the melting and evaporation zone (19.4), the drying of the solids in the drying zone (19.5) with the Discharge of the solids into the extraction shaft (3.20) and removal of the hot gases (3.21) under vacuum (18.12) from the gas dome (3.19).

When changing the direction of rotation (A and B) of the screw shovel in the direction of rotation (B) of the reactor contents (19.8) against the main flow direction (3.13) is promoted. To ensure the discharge of solids (3.22) at least two revolutions in the main flow direction (1.13) must take place after one revolution in the counterflow direction (B).

In the lower third of the melting and evaporation zone (19.4) is the mixing zone (19.4.1) in which the screw shovel (1.5) by introducing transverse forces mixing (19.7) of the not yet liquefied reactor contents (19.8) takes place.

The tube of the reactor jacket (19.8) in the region of the melting and evaporation zone (19.4) is covered by a heating jacket (19.11) in which a heating medium (4.15) flows in countercurrent to the main flow direction (1.13) of the reactor contents (19.8).

The heating medium (4.15) is advantageously made of liquefied sodium chloride, which is also referred to as a thermal salt and its solidification point at +168 ° C and the maximum operating temperature at +620 ° C and is operated without pressure, by the heat input (19.9) can the reactor contents (19.8) are heated to a maximum of +580 ° C.

When using heat transfer oils (thermal oil), the maximum operating temperature is +400 ° C and the operating pressure is 20 bar.

Since most of the hydrocarbon compounds and lignin evaporate at +340 ° C, the single-tube evaporation reactor (19) is operated in the range of maximum +420 ° C. Below the set level (19.3), the liquefied reactor contents (19.8) are thoroughly mixed by the rising gas bubbles (19.10).

Per m <3> reactor contents (19.8) form at a temperature of +400 ° C about 65 m 3 / hour cracking gases with a weight of about 4.6 kg / Nm <3>, which the gas dome ( 3.19) as hot gases (3.21).

The heat generation (4) is shown here as lying boiler with a tube bundle heat exchanger (4.4) which separates the first pulling channel (4.13) from the second pulling channel (4.14). With a screw circulation pump (4.7), the heating medium (4.15) is circulated and conveyed into the heating medium inlet (4.5) of the evaporation reactor (19).

The Heizmediumausgang (4.6) is located in the immediate vicinity of the heat generation (4) and flows in free fall in the expansion vessel. The fuel gases (4.1) for the operation of the heat generation consist of the non-condensable portions of the hot gases (3.21).

The dry exhaust gases (1.7) leave the heat generation (4) via the hot gas channel (1.8) and are fed as drying energy to the dryer (1). The function of the dryer (1) is described in detail in FIG.

FIG. 12 shows a structure of the pyrolysis device which is described in detail in FIG. 1, with the exception that the heat input (4.18) into the active surface (3.47) as described in FIG. 11, via a liquid heating medium (4.15), which is heated by the heat generation (4) and the burner (4.2) is operated with its own fuel gases (4.1). The dry exhaust gases (1.7) from the heat generation (4) are fed to the dryer (1) as drying energy.

The dry material (1.13) leaves the dryer and is introduced through the filling device (2) in the extruder (3.7).

The compressed stream (3.44) is pressed in the form of a press strand (3.8) with the contact pressure generated by the extruder (3.14) against the hot active surface (3.4.7) of the heating plate (18.6) and evaporated. The resulting hot gases (3.21) are drawn off from the gas dome (3.19) via the applied vacuum (18.12) and the solids (3.22) leave the pyrolysis reactor (3) via the extraction shaft (3.20).

FIGS. 13, 14 and 15 show a horizontal evaporation reactor (19) with an inclination (19.6) of between 5 and 10 degrees relative to the horizontal (19.6.1), the inclination (19.6) of the different material flows of the Material entry (19.12) be adapted, such as at the dried fraction of household waste at about 5 degrees and at the dried fraction of mixed plastics at 10 degrees.

The reactor shell (19.1) encloses the screw shovel (1.5) whose operation and construction in Figs. 9 to 11 described in detail and by the drive (1.4) via the drive shaft passage (1.4.1) and the shaft seal (1.4.2 ) is moved.

In the middle (24) of the evaporation reactor (19) is a discharge shaft (19.13) which comprises the reactor shell (19.1). The reactor jacket (19.1) is opened in the upper third to the cutout width (27) in which the cutout height (28) is three quarters of the pipe diameter of the evaporation reactor (19) and the cut length (26) the pipe diameter (26.1) of the screw pump (19a · n) , The distance (27.1) between the outer wall of the exhaust duct (19.13) and the reactor jacket (19.1) is at most one quarter of the pipe diameter (26.1).

By this arrangement flows over the liquid Umlaufgut (19.15) in the upper part of the reactor shell (19.1) and the heavier impurities in the form of solids (3.22) remain in the lower part of the reactor shell (19.1).

The level (19.3) of the level in the exhaust duct (19.13) is set via the level measurement (19.14) whose control signals the filling device (19b) on and off, while the level (19.3) is always above the cut-out width (27) so that is ensured that the Umlaufgut (19.15) sucked by the underlying screw pump (19a · n) and back into the evaporation reactor (19) is conveyed.

The worm pump is also arranged inclined, while the inclination (19.6) to the horizontal (19.6.1) is between two to four degrees. Due to this inclination (19.6), gas bubbles (19.10) are constantly conveyed upwards in the main flow direction (3.13) and thus sustainably prevent cavitation.

The evaporation reactor (19) and the screw pump (19a · n) both have a heating jacket (19.11) comprising the reactor jacket (19.1) and the pump tube (19.16), in which the heating medium (4.15) flows in countercurrent (4.21) to the Main flow direction (3.13) of the melt (19.17) flows and introduces the heat input (19.9) in the melt (19.17).

The material entry (19.12) in the evaporation reactor (19) via the material input device (19b) with the loading device (6.9) which is arranged centrally (23) between the exhaust duct (19.13) and the lower reactor end (19.18).

The registered fresh material (19.19) is immediately dissolved by the liquefied Umlaufgut (19.15) in the form of a hot melt (19.20) and heated by the mixing (19.7) with the hot Umlaufgut (19.15), wherein the mixing ratio between the cold Frischgut (19.19) and about +350 ° C hot circulating material (19.15) is about 1 to 10 parts.

The dry material (1.18) introduced into the material introduction device (19b) is removed from the feed container (1.6.3) with a stuffing spiral and pressed against a compression strand (3.8), which is formed by the friction on the casing tube (1.3) and before Pressing area (20) the conveyor spiral (2.4) ends.

In the middle between the Sicherheitsabsperrschieber (6.6) and the entry tank (1.6.3) is the nitrogen entry (6.5) which is controlled by the solenoid valve (6.4).

When the geared motor (1.4) which drives the spiral (2.4) starts, the magnetic valve is opened, so that with a fresh material (19.19) supplied to 1 m <3>, there is about 1 m <3> nitrogen with an overpressure of about 100 mbar blown.

At the same time, the pressure build-up in the extrudate (3.8) presses out the oxygen and nitrogen mixture (6.7) and leaves the plug spiral (6.8) via the through opening (6.1.2) in the selenium spiral (2.4) and exits as exhaust air mixture ( 6.11) the entry tank (6.11). In Fig. 15, the structure of the selenium spiral (2.4) is shown.

Via the press control (6.12) all necessary steps are set and monitored, e.g. Speed, contact pressure, quantity supply via the level measurement (19.14), nitrogen entry as well as emergency shutdown and closing of the gate valve (6.6).

In the loading device (6.9) two functions are fulfilled by the continuous conveyor spiral (2.4) as follows: a) The length (21) is designed as a selenium spiral (2.4) and raspert the pressed strand (3.8) in the region of the compacted zone (20.1) and pushes the loosened fresh material (19.19) in the main conveying direction (13.13) in the conveying zone (22 ). b) In this conveying zone (22) the spiral (2.4) is provided with a central tube (2.4.1) and thus fulfills the function of a screw spindle (4.11) which below the level (19.3) protrudes into the hot melt (19.17) and with Help of the screw spindle (4.11), which can press into this zone already prone to liquefaction fresh goods (19.19).

After the exhaust duct, the evaporation section (25) begins in which the hot gases (3.21) gas bubbles (19.10) form which mix the reactor contents sustainably by the rising gas (19.7)

The hot gases (3.21) leave the evaporation reactor (19) as superheated steam or so-called cracking gases (19.21) via the gas dome (3.19) which is connected by the downstream cooling and condensation under vacuum (18.12).

In the subsequent drying zone (25.1) which is above the level (19.3), the residues such as solids (3.22), slag (3.23) and charcoal (3.24) dried and the screw shovel (1.5) as dry material in the Discharge shaft (3.20) supported.

The withdrawal shaft (3.20) is provided with a lock (6.1) which is rendered inert via the nitrogen entry (6.5). The shut-off devices consist of two pieces of gas-tight shut-off valves (6.2) provided with drive elements which are opened and closed via the control unit (6.3) d via time control, as well as the solenoid valve (6.4) for the nitrogen entry (6.5) activated, so that during the solids discharge (3.22) no atmospheric oxygen is introduced into the evaporation reactor (19).

LIST OF REFERENCE NUMBERS

[0107] <tb> X <SEP> Scope of the claims, designation in Fig. 6 and 7 <Tb> 1 <September> dryer <Tb> 1.1 <September> Nassguteintrag <Tb> 1.2 <September> feed connection <Tb> 1.3 <September> casing <Tb> 1.4 <September> Drive <Tb> 1.4.1 <September> drive shaft bushing <Tb> 1.4.2 <September> shaft seal <Tb> 1.5 <September> Screws Schaufler <Tb> 1.5.1 <September> blades <Tb> 1.5.2 <September> spiral <Tb> 1.6 <September> packing material <Tb> 1.6.1 <September> Material sales <Tb> 1.6.2 <September> bulk direction <Tb> 1.6.3 <September> entry container <tb> A <SEP> Direction of rotation A <tb> B <SEP> Direction of rotation B <tb> 1.7 <SEP> Dry exhaust gases <Tb> 1.7.1 <September> exhaust gas flow <Tb> 1.8 <September> hot-gas duct <Tb> 1.9 <September> surface <Tb> 1.10 <September> steam <tb> 1.11 <SEP> Moist water vapor <Tb> 1.12 <September> wet gas channel <Tb> 1.13 <September> dry material <Tb> 1.14 <September> material flow direction <Tb> 1.15 <September> cocurrent <Tb> 1.16 <September> countercurrent <Tb> 1.17 <September> Trockengutaustrag <Tb> 1.18 <September> dry material <Tb> 2 <September> filling <Tb> 2.1 <September> filling pipe <Tb> 2.3 <September> Drive <Tb> 2.4 <September> spiral <Tb> 2.4.1 <September> central tube <Tb> 2.5 <September> conveying direction <Tb> 3 <September> pyrolysis <Tb> 3.1 <September> filler 'Tb> 3.1.1 <September> Material entry <Tb> 3.2 <September> reactor shell <Tb> 3.3 <September> cooling jacket <Tb> 3.3.1 <September> jacketed <Tb> 3.4 <September> cooling water inlet <Tb> 3.5 <September> cooling water outlet <Tb> 3.6 <September> Drive <Tb> 3.7 <September> plodder <Tb> 3.8 <September> Press strand <Tb> 3.13 <September> main current direction <Tb> 3.14 <September> pressure <Tb> 3.14.1 <September> backpressure <Tb> 3.15 <September> Material Flow <tb> 3.15.1 <SEP> Material feed <Tb> 3.16 <September> metal compensator <Tb> 3.17 <September> gap adjustment <Tb> 3.18 <September> adjustment device <Tb> 3.19 <September> gas dome <Tb> 3.20 <September> uptake shaft <Tb> 3.21 <September> hot gases <Tb> 3.22 <September> solids <Tb> 3.23 <September> slag <Tb> 3.24 <September> Charcoal <Tb> 3.25 <September> jacket sheet <Tb> 3.30 <September> packing material <Tb> 3.30.1 <September> press shaft <Tb> 3.31 <September> casing <Tb> 3:32 <September> Piston <Tb> 3:33 <September> Hub <Tb> 3:34 <September> cone <tb> 3.35 <SEP> Guidance and Storage <Tb> 3:36 <September> rotary motion <Tb> 3:37 <September> mouth <Tb> 3.37.1 <September> Pipe <Tb> 3.37.2 <September> polygon <Tb> 3:38 <September> gear <Tb> 3:39 <September> pinion <Tb> 3:40 <September> Storage <Tb> 3:41 <September> gearmotor <Tb> 3:42 <September> Partition <Tb> 3.42.1 <September> guideway <Tb> 3.42.2 <September> adjustment <Tb> 3:43 <September> Groove <tb> 3.44 <SEP> Compressed material flow <Tb> 3:45 <September> scraping edge <Tb> 3:46 <September> carbon structure <Tb> 3:47 <September> effective area <Tb> 4 <September> heat generation <Tb> 4.1 <September> combustion gases <Tb> 4.2 <September> burner <Tb> 4.3 <September> burner flame <Tb> 4.4 <September> tube heat exchanger <Tb> 4.5 <September> Heizmediumeingang <Tb> 4.6 <September> Heizmediumausgang <Tb> 4.7 <September> Screws circulation pump <Tb> 4.8 <September> Drive <tb> 4.9 <SEP> Storage and sealing <Tb> 4.11 <September> Screw <Tb> 4.12 <Sept.> casing <tb> 4.13 <SEP> First train channel <tb> 4.14 <SEP> Second train channel <Tb> 4.15 <September> heating medium <Tb> 16.4 <September> upheaval <Tb> 4.17 <September> Level <Tb> 4.18 <September> heat input <Tb> 4.18.1 <September> Expansion vessel <Tb> 4.19 <September> boiler casing <Tb> 4.20 <September> filler <Tb> 4.21 <September> Heizmediumsströmung <Tb> 4.22 <September> Temperature Probe <Tb> 4.23 <September> nitrogen blanketing <Tb> 4.24 <September> flue outlet <Tb> 4.25 <September> hot gases <Tb> 5 <September> sludge <Tb> 6 <September> solids <Tb> 6.1 <September> sluice <Tb> 6.2 <September> Gate Valve <Tb> 6.3 <September> control unit <Tb> 6.4 <September> solenoid valve <Tb> 6.5 <September> Nitrogen <Tb> 6.6 <September> Gate Valve <tb> 6.7 <SEP> Air Oxygen and Nitrogen Mixture <Tb> 6.8 <September> Stopfspirale <Tb> 6.9 <September> loader <Tb> 6.10 <September> friction <Tb> 6.11 <September> air mixture <Tb> 6.12 <September> opening <Tb> 6.13 <September> press control <tb> 7 <SEP> Thermal Oxidation <Tb> 7.1 <September> Guns <Tb> 7.2 <September> Oxygen <tb> 7.3 <SEP> Air or oxygen <Tb> 7.4 <September> inert substances <Tb> 7.5 <September> hot gases <Tb> 8 <September> slag cooler <Tb> 8.1 <September> cooling water inlet <Tb> 8.2 <September> cooling water outlet <Tb> 8.3 <September> slag <Tb> 8.4 <September> cooling jacket <Tb> 9 <September> capacitor <tb> 9.1 <SEP> Lye or acid <Tb> 9.2 <September> Circulation 'Tb> 9.3 <September> cooler <Tb> 9.4 <September> spray cone <Tb> 9.5 <September> condensate discharge <Tb> 9.6 <September> cooling water inlet <Tb> 9.7 <September> cooling water outlet <Tb> 10 <September> biofilter <Tb> 10.1 <September> Blower <Tb> 10.2 <September> Horn <Tb> 10.3 <September> pack <tb> 10.4 <SEP> Purified exhaust air <Tb> 11 <September> partial condenser <Tb> 11.1 <September> cooling water inlet <Tb> 11.2 <September> cooling water outlet <Tb> 11.3 <September> condensates <Tb> 11.4 <September> gas outlet <Tb> 12 <September> spray cooler <Tb> 12.1 <September> Sprühkegelteller <Tb> 12.2 <September> Liquid fuels 'Tb> 12.3 <Sept.> Circulation <Tb> 12.4 <September> cooler <Tb> 12.5 <September> cooling water inlet <Tb> 12.6 <September> cooling water outlet <Tb> 12.7 <September> Overflow <Tb> 12.8 <September> liquid jet pump <tb> 12.9 <SEP> Non-condensable gases <Tb> 13 <September> light liquid separation unit <Tb> 13.1 <September> Water <Tb> 13.2 <September> Liquid fuels <Tb> 14 <September> liquid fuel storage <Tb> 14.2 <September> liquid fuel <Tb> 15 <September> gas storage facility <Tb> 15.1 <September> combustion gases <Tb> 16 <September> CHP plant <Tb> 16.1 <September> Generator <Tb> 2.16 <September> Power supply <Tb> 16.3 <September> Hot water supply <Tb> 16.4 <September> Hot water return <Tb> 16.5 <September> exhaust <Tb> 17 <September> Cooling Water Central <Tb> 18 <September> evaporation reactor <Tb> 18.1 <September> carrier plate <Tb> 18.1.1 <September> Induction Heating <Tb> 18.2 <September> rods <Tb> 18.3 <September> travel <Tb> 18.4 <September> mounting plate <Tb> 18.5 <September> inductor <Tb> 18.5.1 <September> induction coil <Tb> 18.6 <September> hotplate <Tb> 18.6.1 <September> surface <Tb> 18.8 <September> low voltage distribution <tb> 18.9 <SEP> Electrical power distribution <Tb> 18.10 <September> induction generator <Tb> 18.10.1 <September> Power Entry <Tb> 18.10.2 <September> Energy outlet <Tb> 18.11.1 <September> cooling water inlet <Tb> 18.11.2 <September> cooling water outlet <Tb> 18.12 <September> vacuum <Tb> 18:13 <September> spiral spring <tb> 18.13.1 <SEP> Tensioned Sprial Spring <Tb> 18:14 <September> clamping disc <Tb> 18:15 <September> bias <Tb> 18:16 <September> clamping screw <Tb> 18:17 <September> Print Setting <Tb> 18:18 <September> rest position <Tb> 18:19 <September> pressure situation <Tb> 18:20 <September> feed direction <Tb> 18:21 <September> push-back direction <Tb> 18:22 <September> placement angle <Tb> 19 <September> evaporation reactor <Tb> 19 "n <September> screw pump <Tb> 19b <September> filling <Tb> 19.1 <September> reactor shell <Tb> 19.1.1 <September> reactor chamber <Tb> 19.2 <September> Drive <Tb> 19.3 <September> Level <tb> 19.4 <SEP> Melting and Evaporation Zone <Tb> 19.4.1 <September> mixing zone <Tb> 19.5 <September> drying zone <Tb> 19.6 <September> inclination <Tb> 19.6.1 <September> Horizontal <Tb> 19.7 <September> mixing <Tb> 19.8 <September> reactor contents <Tb> 19.9 <September> heat input <Tb> 19.10 <September> gas bubbles <Tb> 19.11 <September> heating jacket <Tb> 19.12 <September> Material entry <Tb> 19:13 <September> uptake shaft <Tb> 19:14 <September> Level gauges <Tb> 19:15 <September> circulation material <Tb> 19:16 <September> pump tube <Tb> 19:17 <September> Melt <Tb> 19:18 <September> reactor end <Tb> 19:19 <September> fresh material <tb> 19.20 <SEP> Hot melt <Tb> 19:21 <September> Crack gases <Tb> 20 <September> Press area <tb> 20a <SEP> Compressed Zone <Tb> 21 <September> Length <Tb> 22 <September> production zone <Tb> 23 <September> Centered <Tb> 24 <September> mid <Tb> 25 <September> evaporation path <Tb> 25.1 <September> drying zone <Tb> 26 <September> cutting length <Tb> 26.1 <September> pipe diameter <Tb> 27 <September> Section Width <Tb> 27.1 <September> distance <Tb> 28 <September> cutting height <Tb> 29 <September> cutout opening

Claims (39)

1. A process for melting and evaporating (3.8) lignin, cellulose, and carbonaceous streams (3.15) or mixtures thereof, wherein the dryer (1), the filling device (2), the pyrolysis reactor (3) and the heat and power generation (4 and 16) together form a closed and interconnected unit in terms of material flow and energy and via a wet material entry (1.1), the entry of the fuel gases (4.1) and the discharge of the solids (3.22) of the hot gases (3.21) and the moist water vapor (1.11 ). 2. The method according to claim 1, wherein the stream (3.15) is pressed under oxygen exclusion with an extruder (3.7) via a rotating orifice (3.37), against a fixed heating plate (18.6). 3. The method according to claims 2 and 3, wherein the contact pressure (3.14) of the material flow (3.15) on the hot plate (18.6) between 1200 to 1500 kg / cm <2>. 4. The method of claim 2 and 3, wherein the electrical energy to excite the induction coil (18.5) and the entire process control (1-19) via a CHP plant (16) with coupled generator (16.1) takes place and the fuel for operation the CHP plant (16) and the heat generation (4) from the self-produced non-condensable fuel gases (15.1) consists. 5. The method according to claim 3 and 4, wherein the fixed heating plate (18.6) via an induction coil (18.5) is heated to a heat range between 400 ° C to 1200 ° C. 6. The method of claim 2, 4 and 21, wherein the dry material (1.13) via the filling device (2) with the extruder (3.7) is pressed into the evaporation reactor (19). 7. The method of claim 2, 4 and 26, wherein the dry material (1.18) via the filling device (19b) in the evaporation reactor (19) is pressed. 8. The method according to claim 2 and 3, wherein the active surface (3.47) of the heating plate (18.6) is at most 350 cm2. 9. The method according to claims 2 and 3, wherein the mouth pipe (3.37) as a round tube (3.37.1) or as a square or polygonal (3.37.2) is formed. 10. The method according to claims 3 and 4, wherein the contact pressure (3.14) and the temperature of the hot plate (18.6), based on the composition of the material flow (3.15) and by regulating these three parameters, the desired amount of energy products in the form of Liquid fuels (14.2), fuel gases (15.1) and the accumulation of solids (3.22) such as slag (3.23) and charcoal (3.24). 11. The method according to claims 1 and 5, wherein the dry exhaust gases (16.5) from the power plant (16) for drying the stream (3.15) in the dryer (1) are consulted. 12. The method according to claim 11, wherein the material bed (1.6) in the dryer (1) by the screw shovel (1.5) in the material flow direction (1.14) moves and simultaneously by changing the direction of rotation (A and B) with respect to the direction of the exhaust gas flow (1.7 .1) the material bed (1.6) in Mitstrom (1.15) or countercurrent (1.16) is performed. 13. The method according to claims 11 and 12, wherein by the blades (1.5.1) the material bed (1.6) by the changing direction of rotation (A and B) and the material turnover (1.6.1) constantly new surfaces (1.9) are created, which are dried with the hot exhaust gas flow (1.7.1). 14. The method according to claim 2, wherein the gap adjustment (3.17) between the mouth (3.37) via the adjusting device (3.18) takes place. 15. The method according to claims 2 and 9, wherein with the rotary movement (3.36) of the mouth pipe (3.37) through the partition (3.42) or grooves (3.43) in the mouth pipe (3.37), the compacted material bed (3.30) is rotated. 16. The method of claim 9, 15 and 16, wherein the partition (3.42) consists of a non-electrically conductive inert material. 17. The method according to claims 2 and 11, wherein the contact pressure (3.14) and the material feed (3.15.1) is pulsating and the adjustable frequency of the strokes (3.33) between 0.5 to 5 seconds. 18. The method according to claims 10 and 15 to 17, wherein the partition wall (3.42) is pressed via an adjusting device (3.42.2) against the heating plate (18.6) and with the scraping edge (3.45) the surface (18.6.1) of the heating plate (18.6) from caking such as carbon buildup (3.46) cleans. 19. The method according to claims 5 and 8, wherein depending on the specific heat content of the bed of material (3.30), the energy input into the heating plate (18.6) between 100 watts and 800 watts times second. 20. The method according to claim 17 and 18, wherein material beds (3.30) are cooled with thermoplastic properties by the cooling jacket (3.3). 21. The method according to claims 2 to 5, wherein the hot gases (3.21) under vacuum (18.12) are withdrawn from the gas dome (3.19). 22. The method according to claims 2 and 4, wherein the extrudate (3.8) from the extruder (3.7) has a density of at least 1.2 kg per dm <3>. 23. The method according to claims 3 and 17, wherein within a stroke (3.33) the heating surface (18.6) with the mounting plate (18.4) in the feed direction (18.20) is pressed and by the bias (18.15) with simultaneous melting of the extrudate (3.8 ) is pressed into the end position via the reverse direction (18.12). 24. The method according to claim 23, wherein the contact pressure (3.14) is always greater than the pressure of the opposing bias voltage (18.15). 25. The method according to claims 1 and 7, characterized in that in the evaporation reactor (19) the material entry (3.1.1), the melting and evaporation (19.4) and the drying of the slag (19.7) in a reactor space (19.1.1) under vacuum ( 18.12) 26. The method according to claim 25, wherein the material entry (3.11) into the inclined (19.6) evaporation reactor (19) at the lower end and the deduction of the solids (3.22) and the hot gases (3.21) at the top, the material entry (3.11) takes place opposite end. 27. The method according to claim 7 and 25, wherein in the middle (24) of the inclined (19.6) evaporation reactor (19) via the take-off shaft (19.13) hot melt (19.17) is withdrawn as Umlaufgut (19.13). 28. The process according to claim 27, wherein the hot melt (19.17) overflows over the overhead cutout opening (29) and the solids (3.22) accumulated in the bottom of the evaporation reactor (19) remain there and are discharged through the slow speed of the screw shovel (1.5) become. 29. The method according to claim 27 and 28, wherein the hot melt (19.17) sucked by the underlying screw pump (19a) and is conveyed into the lower end of the evaporation reactor (19). 30. The method of claim 28 and 29, wherein the screw pump (19 a) in the opposite direction to the evaporation reactor inclined (19.6) is arranged. 31. The method of claim 29 and 30, wherein in the middle (24) of the evaporation reactor (19) via the discharge shaft (19.13), the screw pump (19a) and the center (2.3) arranged Frischguteintrag (19.19) by the Umlaufgut (19.15 ), a circulation flow is established, which causes a thorough mixing (19.7) of the hot melt (19.17) with the cold fresh material (19.19) and shortens the melting process via the dynamic heat input (19.9). 32. The method according to claim 29, 30 and 31, wherein a plurality of screw pumps (19a · n) are used in parallel side by side for the circulation of the circulating material (19.15). 33. The method according to claim 7 and 25, wherein the level in the evaporation reactor (19) via the level measurement (19.14) takes place with which the filling device is driven. 34. Apparatus for carrying out the method according to claim 25, wherein the material transport in the reactor by a conveyor in the form of a screw shovel (1.5), which extends over the entire heated effective length of the evaporation reactor (19). 35. Apparatus for carrying out the method according to claim 34, wherein the drive (19.2) for the screw shovel (1.5) is attached to the overhead end of the evaporation reactor. 36. Apparatus for carrying out the method according to claim 34, wherein by cyclically changing the direction of rotation (A and B) of the screw shovel (1.5), the reactor contents (19.8) are mixed (19.7) and thereby the heat input (19.9) is accelerated. 37. Apparatus for carrying out the method according to claim 34 and 36, wherein dried in the drying zone (9.5), the inert residues and non-cracked carbons through the hot surfaces (18.6.1) and with the screw shovel (1.5) as dry solids (3.22 ) is conveyed to the outlet shaft (3.20). 38. Apparatus for carrying out the method according to claim 36 and 37, wherein the screw shovel (1.5) of the heated reactor jacket (19.1) is cleaned of deposits and caking. 39. Apparatus for carrying out the method according to claim 36 and 38, wherein the spirals (1.5.2) of the screw shovel (1.5) by the profiles of the blades (1.5.1) are kept dimensionally stable.