Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
  • F23J15/00—Arrangements of devices for treating smoke or fumes
  • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
  • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
  • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
  • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
  • B09C—RECLAMATION OF CONTAMINATED SOIL
  • B09C1/00—Reclamation of contaminated soil
  • B09C1/06—Reclamation of contaminated soil thermally
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
  • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
  • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
  • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
  • F23G7/14—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of contaminated soil, e.g. by oil
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2201/00—Pretreatment
  • F23G2201/40—Gasification
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2209/00—Specific waste
  • F23G2209/10—Liquid waste
  • F23G2209/102—Waste oil
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2209/00—Specific waste
  • F23G2209/26—Biowaste
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2209/00—Specific waste
  • F23G2209/26—Biowaste
  • F23G2209/261—Woodwaste
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2209/00—Specific waste
  • F23G2209/30—Solid combustion residues, e.g. bottom or flyash
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
  • F23J2215/00—Preventing emissions
  • F23J2215/20—Sulfur; Compounds thereof
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
  • F23J2215/00—Preventing emissions
  • F23J2215/30—Halogen; Compounds thereof
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
  • F23J2217/00—Intercepting solids
  • F23J2217/10—Intercepting solids by filters
  • F23J2217/105—Granular bed
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
  • F23J2219/00—Treatment devices
  • F23J2219/60—Sorption with dry devices, e.g. beds

Definitions

• the invention relates to a method for the treatment of gasification material according to the features in the preamble of claim 1.
• the invention is directed to a device for the thermal treatment of gasification material according to the features in the preamble of claims 4 to 6.
• the complete conversion of the process gas generated in the gasification process into a burned-out odorless flue gas is carried out in a largely linear ceramic flame channel.
• the flame channel extends between a fixed bed gasifier with a vertical reactor space and a boiler of a heating system for generating heating and / or process heat.
• the cracking of the high molecular tarry and oily constituents contained in the process gas at temperatures of 950 ° C.
• the older a fossil fuel is as a gasification product or the more complex the composition of a gasification product, the more problematic the difficulties in converting the gasification products of the gasification product.
• the residence time of the process gas in the flame channel plays an important role here. This is determined by the complexity of the high molecular weight compounds in the process gas and the complexity of their conversion into low molecular weight compounds. Consequently, depending on the composition of the process gases, the length of the flame channel should be adaptable accordingly. Any change in length of the known almost linear flame channel is, for. B. in view of the problems that arise with respect to the available space not easily possible or sensible.
• the object of the invention is to improve both the method required in the preamble of claim 1 and the device described in the preamble of claims 4 to 6 with regard to the process flexibility and the expansion of the acceptance of problematic gasification material in particular, and in addition to using simple means automatable process technology to ensure a mode of operation of the reactor that is independent of the nature of the gasification material and that the substance-related emission development is safely controlled.
• Such a construction allows a sufficiently long flame channel to be provided in the smallest space, in which, in addition to the reaction-kinetically favorable turbulence, the residence time of process gases with even complex, high-molecular compounds can be controlled in such a way that their tarry and oily beings ⁇ components are gradually converted into low-molecular compounds by cracking and their complete oxidation into a burned-out odorless flue gas can be guaranteed.
• the flue gases generated in this way pass from the labyrinth flame channel into a waste heat boiler, in particular a three-pass waste heat boiler, in which the heat generated during the combustion and inerting of the smoke gases can be used effectively and largely energetically.
• Another advantage of the method according to the invention is that even extremely high concentrations of pollutants in the gasification material, which could possibly exceed permissible emission values, can be reacted to in a targeted manner.
• a highly reactive dry adsorbent for example in the form of a highly reactive powdered lime hydrate product, is metered into the flue gas stream by means of suitable metering and reaction vessels or devices. This secondary epulfurization or dechlorination measure is dependent on the location where the dry adsorbent is introduced, on the temperature of the flue gas generated, at which, for. B.
• the greatest possible SO2 - or HC1 or other halogen emission reduction effect is achieved and, among other things, the least possible effort for the subsequent dedusting of the flue gases to be carried out as a result of dry adsorption results.
• the dedusting of the flue gases behind the waste heat boiler can be carried out with the help of candle, hose or bulk filters. These are filter systems in which not only problem-free, ie reliable dedusting and regular cleaning is guaranteed, but also the post-desulfurization or post-dechlorination effect with the aid of the registered but not yet fully reacted or unchanged material Dry adsorbent can be used in the so-called filter cake.
• the core of the embodiment according to claim 2, which further develops the idea of the invention, is the measure of deliberately moving the gasification material downwards in a comparatively thin bed layer on the way from the feed point to the combustion or slag zones in a tilted reactor. that a reaction zone structure can be built up several times in succession in a stationary phase, that is to say with the gasification material at rest, as is usually formed in a pure countercurrent gasifier, which is then subsequently destroyed and shifted again in a feed phase.
• reaction zone structure of the gasification material is torn open or loosened and the mixed gasification material rolling itself over or over in the longitudinal direction of the reactor. transported space. Following this feed phase, a new structure is formed in a further stationary phase of reaction zones customary in countercurrent gasification.
• the cyclical (batch or zone-wise) and also temporally successive tearing of the reaction zone structures, the shifting of the gasification material from one stationary phase to the next stationary phase while rolling over and overturning the gasification material with simultaneous mixing of the reaction zones promotes the desired coke formation and the gasification of the
• the gasifying agent is introduced in cross-flow in substantially equal quantities, it penetrates the
• the cyclical shifting and shifting of the gasification material as well as the formation of a reaction zone structure in a stationary phase, but in ever decreasing thickness of the bed layer, has the advantageous consequence that at no point in the reactor space itself is extremely problematic gasification material with low ash melting point can bake, sinter, glue or coagulate into large slag chunks on the walls of the reactor chamber. It is torn open, loosened and broken again and again during the shifting phases before processes that disrupt the gasification process become effective. As a result, the entire gasification product takes part in the chemical reactions taking place in parallel during the gasification process at every point in the reactor space. In this way, after a number of alternating successive stationary phases and feed phases at the lower end of the reactor space, the gasification material is completely converted into an inert residue and into clear process gas.
• the gasification agent which in particular consists of atmospheric oxygen, but can also consist of oxygen-enriched air or " air-water vapor or oxygen-water vapor mixtures or other oxygen carriers, is specifically supplied to the individual length sections of the reactor space in such a way that up to the region the combustion and slag zones are always supplied with almost equal amounts of gasification agent, only in the area of the combustion and slag zone below a larger amount of gasification agent is introduced in order to ensure that sufficiently high temperatures are generated to to ensure the most favorable Boudouard's gasification conditions for high-calorific process gas production.
• the process according to the invention ensures that in each section located behind the feed point of the reactor space, in which the gasification material participates in the thermal reactions of the gasification process taking place, the oxidation zone with constant gasification conditions becomes increasingly thicker compared to the decreasing and finally completely disappearing thickness of the drying, smoldering and reduction zones. Finally, only the oxidation zone and the slag zone and the zone of the cooling ash are present at the lower end of the sloping reactor chamber.
• the process gases are drawn off together from the reactor space and then transferred into the flame channel.
• Variable cycle times and / or cycle intervals not only allow the precise residence time of the gasification material in the stationary phases to be determined depending on the material, but also allow the rate of displacement, that is to say the separation process of a reaction zone previously established during a stationary phase, to be defined, programmed to control if necessary.
• the rate of displacement of the gasification material can be controlled externally.
• Highly thermally reactive biomasses are particularly suitable as carbonaceous additives. These include, for example, low-ash organic residues such as sawdust, milling and shavings as well as wood chips and bark of fine to medium grain. But also alkaline earth-rich residues from food production, such as B. cocoa or peanut shells are suitable as additives. Of course, coke can also be used for the minimum Cf i x setting.
• the required amount of the additive can vary within wide limits depending on the type, nature and composition of the oil-contaminated gasification material to be treated. However, a low water content of the additive is just as advantageous as a possibly high alkalinity of the additive.
• the mixing in of dry adsorbents to the gasification material and to the carbonaceous additives serves to incorporate existing, emerging or reforming, raw material-bound, dissolved or gaseous pollutants, in particular sulfur and chlorine compounds, at the source of their occurrence. It can e.g. B. to lime or hydrated lime products or corresponding other emissions-reducing products, such as dolomite.
• the amount of dry adsorbent required is primarily determined by the content of sulfur and halogen compounds in the oil-contaminated substances.
• the filter dust and the process ash which are produced during the gasification can now be mixed to form the oil-contaminated gasification material.
• the filter dust as a primary additive, fresh dry additive can be saved, since the filter dust has a sufficiently high alkalinity for this. Due to the high pH values of the filter dust and the process ash, a considerable reduction in the ash melting point can also be guaranteed.
• the melting point reduction promoting slagging results essentially from the addition of the dry adsorbent, for example in the form of lime hydrates and dolomite, without the critical dissociation temperatures and conditions for the sulfur and other halogens from the basic solids during drying adsorption resulting new compounds can be achieved.
• the dust separated during the dedusting of the flue gas contains large amounts of unreacted adsorbent.
• This procedure has the advantage, on the one hand, that in the removal of oil-contaminated gasification material, such as oil sludge and / or oil-contaminated soils, no further residual or waste material is produced in addition to the process ash, and, on the other hand, that the unreacted adsorbent during Mixed product can be used for the integration of gaseous pollutants at the source of their creation.
• the operating costs of the thermal multi-stage treatment of delta-contaminated gasification material can be influenced again in a positive sense.
• the dry adsorbent to be added to the mixed product should advantageously be finely ground to a particle size range of considerably smaller than 1/100 mm.
• a first advantageous solution to the objective part of the object on which the invention is based is seen in the features of claim 4.
• the inclination of the reactor space with respect to the horizontal takes place in order to be able to move the gasification material from the feed chute-side feed point in a comparatively thin bed layer in a clockwise direction towards the lower ash zone mechanically and depending on gravity.
• the degree of inclination is determined by the gasification material.
• the reactor space can also be designed to be inclinable.
• the change can be carried out step by step or continuously.
• the division of the reactor base into stationary sections and sections which are relatively movable relative to them allows the gasification material to be left in the idle state several times during the downward movement, depending on its composition, so that the reaction which usually occurs in countercurrent gasification occurs can form zones and, on the other hand, allows the gasification material which tends to cake, sinter or stick to be loosened continuously and the structures of the reaction zones to be mixed again.
• the reactor floor can be moved individually or together in the predetermined cycle of the stationary phases and the feed phases.
• the speed can be uniform or non-uniform.
• the speed of the sections arranged one above the other at a distance can also differ from one another. In any case, however, it is ensured that the gasification material is repeatedly torn open, shifted (circulated) and loosened up in the feed phases, so that new reaction zone structures can form in the stationary phases with the aim of increasing the
• the fixed sections of the reactor floor are expediently formed by grids which are arranged in steps and one above the other.
• the grids preferably extend in each case in a horizontal plane.
• the gasification agent is supplied in the region of the movable sections in cross flow. Subsequently, the gasification agent penetrates the bed of the gasification material upwards in countercurrent.
• the partial amounts of gasifying agent in each movable section are essentially of the same size. In contrast, it is in the area of
• Combustion and slag zone additionally vertically supplied partial amount of gasification agent larger, in order to ensure in this area the most favorable Boudouard gasification conditions with high calorific value process gas generation with gasification conditions with temperatures up to 1000 ° C.
• the gasifying agent can be supplied in any manner. However, the feeds are preferably located laterally or above and below the movable slides.
• The, in particular, horizontal gas outlet connection lies in the hottest area of the reactor space, in order to be able to remove the reaction gases that accumulate and mix here during the gasification process and to avoid a drop in the temperature of the process gas.
• the gas outlet connection can be provided with openings which can be regulated if necessary. Adjustable openings can be used, for example, to supply secondary air. Other openings can also be set up as measuring and / or control points.
• the device according to the invention makes it possible to use not only lumpy and solid gasification material, but in particular also softening gasification material which tends to become dough, with uniform gas flow through the bed.
• the specific throughput of the Reactor increased with simultaneous increase in the outlet temperature of the process gas due to an increase in the gasification speed.
• controlled gasification conditions are ensured by the transition from a material column, which is typical for countercurrent gasification and is difficult to gasify, to cross-flow countercurrent gasification in low reaction zones, some of which are only a few centimeters.
• the degree of carbon conversion and the efficiency of the gasifier are increased, regardless of whether it is sorted or unsorted masses of any grain size of earthy, sticky, fibrous, plate-like, pasty, softening or moist gasification materials of changing composition.
• the upper ceramic wall of the reactor space is preferably provided so that it can move transversely in order to be able to change the cross-section of the reactor space depending on the composition of the gasification material and the gasification conditions that arise, so that the heat emitted by the gasification material optimally returns to it - shines.
• a layer height regulator at the end of the upper wall on the fill-in shaft can prevent freshly placed gasification material from sliding unhindered and in an undefined quantity into the lower area of the reactor space and, among other things, from causing uncontrolled gasification reactions and undesired incomplete conversion of the gasification material used. This is highly undesirable, for example, when using the device for the environmentally friendly disposal of waste and in particular also during the remediation of contaminated sites.
• All movable and immovable wall or floor sections of the reactor room, with the exception of the upper ceramic wall are water-cooled. Such water cooling makes it possible to operate at high temperatures without fear that the gasification material will bake on the walls of the reactor space.
• a further advantage of the solution according to the invention is the higher degree of carbon conversion, the higher efficiency of the gasifier and the throughput which is significantly improved in comparison with corresponding sizes of conventional countercurrent gasifiers.
• the slide is designed in one piece and in one step. If necessary, it can also be formed in several parts and / or in several stages, in particular in three stages.
• the individual steps here also preferably extend over the entire width of the grate and can be divided into individual, closely spaced and individually variably displaceable blocks or modules.
• the steps descend towards the ash discharge opening. They can be graded evenly or unevenly. Your contour can be angular or curved. They are variable and can be shifted in cycles or zones in the direction of the ash discharge opening.
• a box shape of the slide allows suitable cooling to be integrated in a relatively simple manner.
• a slide recess can be provided in the wall opposite the ash discharge opening. In the starting position, the slide is completely in the slide recess. No parts protrude into the reactor shaft.
• the service life of the slide and its guides in the slide recess is increased when the walls and the bottom of the slide recess and thus also the slide guides are cooled.
• Both the feed length of the slide or, if applicable, its sub-blocks or modules, as well as its feed rhythm, are preferably variable. In this way, the movement of the slide can be tailored to the composition of the respective gasification material and its behavior during the gasification process.
• the grates are designed to be flat, as is the case in practice.
• an end curvature is also conceivable, with which in certain situations it is prevented that gasified material gets into the ash discharge in an impermissible manner.
• the burnout plate is advantageously cooled in order to extend its service life and thus also the operating time of the carburetor.
• Water can be used as the coolant.
• the reactor, the grate, the slide and the slide recess can also be water-cooled.
• An in particular water-cooled discharge screw can be arranged in the ash zone of the reactor.
• a third advantageous embodiment of the invention is seen in the features of claim 6.
• the division of the flame channel into a large number of short length sections and their relative assignment in a triaxial configuration makes it possible to provide a sufficiently long flame channel even in the smallest space, in which the residence time of process gases with even complex high-molecular compounds can be controlled in such a targeted manner that their tars and oily constituents can be gradually converted into low-molecular compounds by cracking and their complete oxidation into burnt-out odorless flue gas can be guaranteed.
• the often tortuous, labyrinthine course of the flame channel created by a crossing, looping, winding, ascending and descending, i.e. constantly changing direction, ensures on the one hand the necessary dwell time of the process gas, which is dependent on the gasification material, and on the other hand allows one optimal turbulent and complete mixing of the process gas to be converted with secondary air.
• a further advantage of the labyrinthine course of the flame channel is seen in the fact that laminar flows which form at short notice are torn up again immediately after their formation and converted into turbulence. This achieves the advantage of being able to drive at significantly higher flow speeds than was possible in the known case, but without reducing the quality of the burnout.
• the invention allows the process gases from extremely problematic gasification material after targeted high-temperature cracking of their high-molecular compounds in the course of the tightened environmental protection regulations while observing the respective regulations to reliably and reliably burn out an odorless and pollutant poor flue gas can be converted.
• the length of the flame channel can always be adjusted relatively easily to the nature of the gasification material in question.
• the type of origin and the age of fossil fuels and their derivatives can be specifically taken into account.
• this can be mixed turbulently and completely with the process gas depending on the respective process gas and its composition as well as its combustion behavior.
• the longitudinal sections can form components of predominantly similarly designed and / or interchangeable module bodies.
• Such module bodies can then be put together in a modular manner depending on the complexity of the process gas to be converted.
• flame channels of different lengths can be put together by the user without any problems and, if necessary, can also be exchanged for another configuration.
• the module bodies can be finished segments made of moldable and / or castable ceramic materials. A brick construction is also conceivable.
• a further embodiment of the basic idea according to the invention consists in the features of claim 9.
• Figure 1 is a schematic perspective view of a multi-stage combustion system
• FIG. 2 shows a diagonal bed reactor for the combustion system of FIG. 1 in an enlarged illustration
• FIG. 3 * also in the diagram in an enlarged view a vertical fixed bed reactor for the combustion system de Figure 1;
• FIG. 4 shows a labyrinth-like flame channel suitable for the combustion system in FIG.
• a reactor space 3 is arranged in a reactor 1 which is inclined at an angle ⁇ to the horizontal 2 and which is delimited laterally by vertical walls 4.
• the bottom of the reactor chamber 3 consists of stationary, horizontal grids 5, which are arranged stepwise at a distance from one another, between which transversely movable slides 6 are arranged.
• the slides 6 can be moved together or separately with possibly different or continuous or discontinuous speeds.
• Gratings 5 and slide 6 are water-cooled
• an ash discharge 7 with a discharge screw 8 is arranged behind the lowest grate 5, but with the upper side at approximately the same height.
• a tubular gas discharge nozzle 9 with, in particular controllable, openings 10 for secondary air extends into the reactor space 3.
• Other openings 10, not shown in the drawings, can also be set up as measuring and / or control points.
• the upper wall 11 of the reactor chamber 3 is arranged such that it can be moved as a ceramic vault transversely to the grates 5 in order to be able to change the cross section of the reactor chamber 3 as a function of the material 12 to be gasified and the gasification conditions which arise.
• a layer height regulator 13 is suspended so as to be pivotable about a horizontal axis 14. This layer height controller 13 prevents freshly fed gasification material 12 from slipping freely and in an undefined amount into the lower region of the reactor space 3 via the feed shaft 16 provided with a lock 15.
• the feed 17 for the gasification agent 18, such as in particular atmospheric oxygen, is provided.
• the gasification agent 18 reaches the reactor chamber 3 in a targeted cross flow in almost equal subsets in the area of the slide 6 and additionally in the opposite. flows vertically into the reactor space 3 over the distance 19 between the lowermost grate 5 and the ash discharge 7 in a relatively large amount.
• the gasification material 12 fed in via the feed chute 16 extends in a pouring layer 20 which decreases in height in the longitudinal direction of the reactor chamber 3.
• the Reaction zones 21-24 arising from conventional countercurrent gasification. Feed phases are integrated between the stationary phases, in which the gasification material 12 is displaced mechanically and by gravity in the longitudinal direction of the reactor space 3 by the slide 6. During this shift, the structures of the reaction zones 21-24 which form in the stationary phases are loosened, torn open and rearranged. This prevents problematic gasification material 12, which also tends to sinter, bake or stick, to become locally fixed.
• the entire gasification 12 takes part in the chemical reactions taking place at every point in the reactor space 3 during the gasification process. Because of this procedure, the desired coke formation is promoted with simultaneous gasification of the coke in the reduction zone 22.
• the thickness of the oxidation zone 21 increases continuously in the longitudinal direction of the reactor space 3, while the drying zone 24, the smoldering zone 23 and the reduction zone 22 become thinner and finally disappear completely. At the lower end of the reactor space 3, only the oxidation zone 21 and the slag zone 25 and the layer of cooling ash are then present.
• the process gas resulting from the gasification is transferred via the gas discharge nozzle 9 into a labyrinthine flame channel 62 for complete conversion into burnt-out odorless flue gas (see FIGS. 1, 4 and 5).
• the flame channel 62 is divided into short length sections 26, 27, which are connected to one another in a triaxial configuration.
• the direction of the flame channel 62 is defined by arrows.
• the longitudinal sections 26, 27 are formed in block-shaped module bodies 28 as longitudinal channels and as transverse channels intersecting them at one end of the longitudinal channels.
• Such a module body 28 produced from a castable ceramic mass ⁇ is illustrated in more detail. It can be seen that, depending on the intended use, the longitudinal channels 26 and transverse channels 27 can be closed at the ends by plugs or cover plates 29.
• the channel cross section is arbitrary. In the embodiment, it is angular.
• Length sections 26, 27 and the plugs and / or cover plate 29 are assigned secondary air feeds 30, which can be regulated in a manner not illustrated in any more detail.
• FIG. 4 shows that the module bodies 28 forming the flame channel 62 can be surrounded by a heat-insulating jacket 31.
• Secondary air is possible to mix the process gas and the secondary air turbulently and completely. Where the secondary air is added and how much depends on the composition of the respective process gas and its combustion behavior. The dwell time of the process gas in the
• Flame channel 62 for conversion into completely burned-out, odorless and low-pollutant flue gas can be precisely predetermined and varied by correspondingly assigning module bodies 28.
• 34 dry adsorbents are metered into the flue gas from a bunker 35, for example in the form of highly reactive hydrated lime, in powder form by means of allocation 36 and blowing system 37. The purpose of this is to take into account the pollutant concentrations in the gasification material 12 respectively input into the reactor 1 with regard to the permissible emission values.
• a flue gas filter 38 for example in the form of a bulk filter, is provided behind the input point 34 for the dry adsorbent designed as a mixer.
• a dry adsorbent in granular form is used as bulk material.
• the flue gas cleaning can hereby be carried out even more effectively in the sense of better utilization of the dedusting and post-desulfurization or post-dechlorination effect.
• the gasification material 12 fed into the reactor 1 is in particular earthy and crumbly and is produced in that ⁇ l-contaminated substances of various compositions, such as oil sludge or ⁇ lcontacted soils, in an untreated state with carbonaceous additives, with highly reactive dry adsorbents, filter dust and with process ash be mixed and dispersed. It is advantageous if the process ash obtained during gasification is mixed with the ⁇ l-contaminated substances. Furthermore, the filter outlets can be used as a primary desulfurization additive Oil-contaminated substances are added because they contain large amounts of unreacted adsorbents.
• a fixed bed reactor 1 'according to FIG. 3 can also be used if gasified material 12', such as. B. Chicken manure or tropical hardwoods should be treated.
• FIG. 3 44 denotes the water-cooled housing of the fixed bed gasifier 1 ", which is not shown in detail, with a vertically oriented reactor shaft 45.
• the walls of the reactor shaft 45 are water-cooled.
• the filling device with a material lock for the gasification material 12 ' is illustrated in a greatly simplified representation with the arrow Pf.
• a grate 46 is rigidly integrated, which carries the gasification material 12 'within which the reaction zones, such as drying zone 47, smoldering zone 48, reduction zone 49, oxidation zone 50 and slag zone 51, form during the gasification process.
• the water-cooled grate 46 serves over its entire width as a sliding guide for a three-stage, multi-part slide 52 which, from the initial position within a slide recess 53 in the wall 54 of the reactor shaft 45, transversely to the reactor shaft 45 in the direction of one in the
• Displacement plane of the slide 52 opposite ash discharge opening 55 is displaceable.
• multiplicity is understood to mean a structure in which the slide 52 consists of a plurality of blocks or modules lying next to one another of the same construction but of different widths and differently or variably individually movable.
• the publishers The slide 52 or the blocks or modules can be freely selected and, depending on the gasification material, can be predetermined with regard to the feed length and / or the feed rhythm.
• the slider 52 is box-shaped and provided with water cooling.
• the walls delimiting the slide recess 53 and the floor are also water-cooled.
• gasified material 12 ' which has been burned out and completely converted to ash is used as an inert material from the grate 46 via the ash discharge opening 55 into an ash discharge 56 with an ash discharge .
• Screw 57 is pushed and, on the other hand, after the slide 52 is moved back into the slide recess 53, free spaces are created into which new gasification material 12 'can sink from above.
• the compression of the gasification material 12 ′ which is brought about briefly when the slide 52 is displaced in the direction of the ash discharge opening 55 is irrelevant.
• a water-cooled burn-out plate 60 is arranged below the ash discharge opening 55 in a plane which is also below the grate 46. This ensures that gasification material 12 'which has not yet been completely gasified, but is pushed out by the slide 52, is also fully converted here with a high excess of oxygen.
• the process gas 61 formed during the gasification process is drawn off above the hottest reaction zones 49, 50 via the gas outlet connection 9 and fed to the flame channel 62 according to FIGS. 1 and 2, in which the process gas 61 is then, after gradual cracking, from high-molecular to low-molecular compounds , mainly gases, is completely burned out and converted into odorless, low-pollutant flue gas.

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• Engineering & Computer Science (AREA)
• Environmental & Geological Engineering (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Physics & Mathematics (AREA)
• Thermal Sciences (AREA)
• Life Sciences & Earth Sciences (AREA)
• Soil Sciences (AREA)
• Processing Of Solid Wastes (AREA)
• Gasification And Melting Of Waste (AREA)
• Treating Waste Gases (AREA)

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• 1989
  • 1989-06-07 DE DE3918508A patent/DE3918508C1/de not_active Expired - Fee Related
  • 1989-09-27 WO PCT/DE1989/000607 patent/WO1990015287A1/de not_active Ceased
  • 1989-09-27 EP EP89910822A patent/EP0431077B1/de not_active Expired - Lifetime

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