EP3535356A1 - Gazéificateur multi-étagé à lit de carbone à expansion tourbillonnaire duplex - Google Patents

Gazéificateur multi-étagé à lit de carbone à expansion tourbillonnaire duplex

Info

Publication number
EP3535356A1
EP3535356A1 EP17808306.9A EP17808306A EP3535356A1 EP 3535356 A1 EP3535356 A1 EP 3535356A1 EP 17808306 A EP17808306 A EP 17808306A EP 3535356 A1 EP3535356 A1 EP 3535356A1
Authority
EP
European Patent Office
Prior art keywords
gas
carburetor
gasification
carbon
gasifier
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP17808306.9A
Other languages
German (de)
English (en)
Inventor
Hartwig Streitenberger
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hs Techtransfer Ug (haft-Beschr) & Co KG
Original Assignee
Hs Techtransfer Ug (haft-Beschr) & Co KG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hs Techtransfer Ug (haft-Beschr) & Co KG filed Critical Hs Techtransfer Ug (haft-Beschr) & Co KG
Publication of EP3535356A1 publication Critical patent/EP3535356A1/fr
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/007—Screw type gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/32—Devices for distributing fuel evenly over the bed or for stirring up the fuel bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • the invention relates to an arrangement in the form of a duplex TEK multistage gasifier, i. a multistage turbocharger with a turbulent-expansive carbon bed (TEK), and a method for autothermal operation of such a gasifier in an overall plant for the thermal decomposition of a carbonaceous material having a very high calorific value to a tar-free combustible gasification gas.
  • the product includes high calorific organic and carbonaceous wastes of high calorific value, such as plastics.
  • This device consists of a shaft-like reactor in which the feed, the gaseous gasification agent and the gaseous fuel produced in descending DC are performed.
  • the gasification agent is preheated in gaseous fuel in a shell-type helical countercurrent heat exchanger.
  • This preheated gasification agent is further heated in helical or wavy channels in the ceramic hearth of the reactor and in a movable or fixed, serving as a hearth end in the lower portion of the charge cone-shaped or paraboloidal central body.
  • the grate is formed by a full cone or a hollow cone-shaped annular body, rotatable, vertically displaceable counterpart, which opposite the lower hearth an adjustable annular passage for withdrawal of the generated gaseous fuel and for discharging the solid or liquid reaction products in the form of ash, slag, Left distillation residues.
  • a disadvantage of this technical solution is that the degassing and / or gasification of the solid fuels or waste to a usable tar-free synthesis gas is not complete and not tarry, because the withdrawal of the gaseous fuel in the separation area the annular passage in the conglomerate of liquid reaction products, distillation residues, ashes and slags takes place. The reaction product as gaseous fuel is thus not free of these partial products.
  • the descending DC carburetor is also sensitive to fragmentation of fuel since the adjustable annular and funnel-shaped passage results in bridging due to flow and thereby tends to clog and dislocations. With a larger “annular gap", the fuel falls without the required reaction time in the lower gasification chamber with the residue disposal and there is thus no sufficient thermochemical conversion into a usable fuel gas.Furthermore, it comes in the bulk cone of the annular passage to caking and bonding in the mixture of liquid reaction products , Distillation residues, ashes and slags and consequent process stoppage.
  • this carburetor has a poor part-load behavior, since at partial load, the amount of gasification decreases, the hot zones are smaller and the intermediate zones increase with low temperature. This also increases the tar content in the product gas.
  • a low-tarry product is only produced when a sufficiently high temperature (temperature stability) prevails in the ember bed over the entire cross section of the gasifier and the pyrolysis gases flow through a closed hot reduction zone. This is difficult or impossible to achieve in systems with larger dimensions, especially at part load.
  • a further disadvantage is that the carburettor type according to the disclosure of EP 0 609 802 AI from the process-related uncontrollable residence times to performance reductions in both the gas quality and in the throughput of the fuel leads.
  • DE 199 37 521 A1 discloses a method and a device, in particular for the processing of already partially decomposed waste products.
  • This device consists of a shaft-like, in the lower part funnel-shaped reactor in which the charge of the carbon particles tangentially and the air is introduced axially as a gasification agent and is converted ascending by means of thermochemical reaction to synthesis gas.
  • the frusto-conical bottom part further has a lateral annular gap, through which the air can enter axially into the reactor space and can mix with the carbon-gas mixture. This gas mixture entrains the carbon particles from the solids bed ascending outwards and is converted in the reactor space at up to 1,200 ° C energetically to synthesis gas.
  • the flow falls inwards and calms down, so that the not yet thermally decomposed carbon parts and the ash parts fall back down. There they meet a collecting funnel located in the center, which runs through to the lower area and is disposed of by a screw conveyor.
  • a disadvantage of this technical solution is that the degassing and / or gasification of solid fuels or waste materials to a usable tar-free synthesis gas is not complete and not tarry and the process stability, due to uncontrolled carbon removal with associated deposition and slagging, especially inert on the parts truncated cone-shaped bottom part, adversely affected and thus can lead to blockages and consequently to uncontrollable process standstill.
  • DE 10 2008 058 602 A1 discloses a moving-bed gasifier comprising a carburetor space and a carburetor base, wherein the carburetor space is surrounded by a carburetor jacket and has a synthesis gas outlet at its one, closed end and via its second, open end via the carburetor jacket with the carburetor in connection.
  • a carburetor dome is arranged in the gasifier space in such a way that an annular gap is generated between it and the carburettor jacket and / or the carburetor trough.
  • the carburetor is in its interior formed as a carburetor trough into which an entry device and at least one feed leads, and in this case has a bottom provided with recesses relative to the gasifier chamber, wherein the bottom opens into a central shaft.
  • This carburetor trough is equipped with stirrers, which are rotatably mounted on a stirrer shaft in the carburetor trough.
  • agitator shaft is surrounded by a conveyor, which serves as a kind of overflow for possibly overfilled carburetor trough.
  • a disadvantage of this technical solution is that the degassing and / or gasification of solid fuels or waste materials to a usable tar-free synthesis gas is not complete and not tarry, since the gasification process by process-related and changing thermochemical reactions in the carbon bed, in particular by increasing the inert residues, Uncontrollably subject to strong fluctuations and thus can run unsteady and consequently does not cause complete gasification of the carbon particles.
  • the gasifier according to the disclosure of DE 10 2008 058 602 AI tends in particular by the non-dischargeable agglomerated inert solids to blockages, which leads to process stoppage.
  • DE 10 2009 007 768 AI discloses a thermolysis reactor, which is placed obliquely ascending, with an entry in the lower part and a discharge in the upper part is provided.
  • This reactor further comprises an outer sheath and an inner sheath which form a double sheath, wherein the inner sheath is surrounded by the outer sheath, so that there is a gap between them for receiving a heat carrier.
  • the reactor has a Vergasungsmitteleintrag and a central shaft with delivery tools that promote the registered waste during the pyrolytic process up and it is to convert it to coke.
  • a disadvantage of this technical solution is that the degassing of the solid fuels or waste to a usable tar-free synthesis gas is not complete and not tarry by destroying the existing bed of embers to the emergence of thermolysis reactions during forced movement of the goods, separate Glutnester to process-disturbing hot Spots and the inert substances that collect below can lead to blockages and thus the entire process can come to a standstill.
  • thermolysis rotary reactor with tubular outer jacket, which is horizontally positioned, and has a central shaft with input and Austragswerkmaschineen.
  • a disadvantage of this technical solution is that the material in the central shaft area is only insufficiently conveyed, the gasification agent is not distributed by the process and the gasification agent Shafts beyond that tend to be closures. Consequently, it comes within the property to partial bonds and lumps of incomplete conditioned good with already formed carbon coke and thereby resulting blockages with concomitant Prozes s standstill.
  • DE 199 37 524 A1 discloses an apparatus and a method for the disposal of waste products and waste, the apparatus comprising a container in which the treated waste is thermally treated at up to 900 ° C. This is done by heating and subsequent pyrolysis of the waste by supplying gasification agent. The mixing and locomotion of the material is carried out in the device according to the disclosure of DE 199 37 524 AI by sitting on a shaft paddles.
  • the gasification agent supply takes place via axially distributed in the thermolysis chamber feeders.
  • the energy input via the gasification agent which is introduced via the axially distributed feeds in the pyrolysis holistically spatially and without quantitative distribution, procedurally in the sequence from the entry to the discharge with the residual drying, reduction and Pollution of the waste material is not process-related, which can also lead to partial overheating, hot spots and unintentional combustion.
  • DE 10 2013 015 920 A1 discloses a 3-zone carburettor and a method for operating such a carburettor for the thermal conversion of waste products and wastes.
  • This carburetor comprises a lower part and a casing with an internal carburetor trough with a solids entry on an inclined trough wall, a Störstoffaustrag arranged below, enclosed by a discharge chute for the flow of gasification agent and residue removal, a truncated cone arranged in the upper carburetor part, controllable by means of a flow valve body, and from it derived adaptive gasification zones.
  • the Störstoffaustrag in zone 1 is directly connected to the discharge chute. Due to this direct fluidic and pressure-technical composite, sufficient process-technical overpressure does not build up for a sufficient flow through the carbon bed with the gasification agent and, as a result of the process, leads to partial clumping of the carbon, in particular in the lower tank region. Along with this, the temperature-technical prerequisites for the oxidation reactions, also due to the further supply of the low-temperature carbon in the upper trough area, are not reached in a stable manner.
  • WO 2001051591 A1 discloses a fuel gas generator used for processing slag-rich products.
  • WO 2001051591 Al teaches solution variants to solve the problem of uneven heating in the reactor. For this purpose, the principles of "downstream gasification” and “upstream gasification” are combined.
  • the feedstock is low-slag and possibly tarry fuel, such as wood.
  • the upper part of the reactor serves as a drying and degassing zone for the filled fuel
  • the underlying part which is separated by a degassing from the upper part, serves as a downstream gasification zone.
  • the effluent gasification agent supply takes place for this purpose in a centrally mounted tube in the downstream gasification space, with oxidation zone and subsequent reaction zone.
  • the residual material is flow-equal down, the fuel gas produced is discharged outside the outer edge zone upwards out of the reactor.
  • thermo-chemical conversion of the Fuel lies in the temperature range from approx. 350 ° C to approx. 500 ° C.
  • the required temperature ranges for the conversion of carbon coke are at least about 800 ° C to about 1400 ° C.
  • a disadvantage of all of the above-described technical solutions is that the degassing and / or gasification of solid fuels or waste to a usable tar-free synthesis gas in an apparatus / gasifier is not complete and not tarry, since the gasification process either by process-related and changing thermochemical reactions In the refuse or carbon spill the necessary successive temperature gradations and in particular the required residence times by means of spatial allocation is not justified.
  • a disadvantage of all of the methods described above, moreover, is that they require an external energy supply during operation, that is to say after starting up the system, i. not run autothermally to operate the process of degassing and / or gasification stable.
  • the object of the present invention is to provide a carburettor and a method for operating this carburetor, which avoid the disadvantages of the prior art and the production of a tar-free, combustible gasification gas in a staged autothermal process, without material, fluidic and procedural interruption, with locally determined conversion and gasification stages with defined time, Temperature and Verwirbelungstalkn (Time-Temperature- Turbulence) and dedicated endothermic and exothermic oxidation and reduction reactions in an overall system for the thermal decomposition of an organic carbonaceous material with high calorific value without external energy supply after starting the plant by a recuperative heat utilization allow.
  • the essence of the invention is to provide a duplex TEK multi-stage gasifier comprising a pre-gasifier (VV) and a main gasifier (HV).
  • VV pre-gasifier
  • HV main gasifier
  • This duplex TEK multistage gasifier is provided with a downstream heat exchanger cyclone, a main heat exchanger, a gasification mixing section comprising an oxygen pre-heater and control lines, a gasifier heater, a hot gas generator, and a process fan, and may be used in an overall plant be integrated for the thermal decomposition of a carbonaceous material with a very high calorific value to a tar-free combustible gasification gas.
  • the material, pressure, gas and flow interconnected primary and main carburettors of the Duplex-TEK multi-stage carburetor are operated without physical separation and are linked to an integrated process control and regulation unit in terms of data and information.
  • the duplex TEK multi-stage gasifier according to the invention is advantageously operated in an overall system together with the downstream components and an integrated process control and regulating unit controlling all components in order to avoid all the disadvantages of the prior art.
  • the pre-carburettor (VV) of this duplex TEK multi-stage carburetor is oriented horizontally and is characterized in its operating condition by
  • the main carburetor (HV) of this duplex TEK multi-stage carburetor is oriented vertically and is characterized in its operating condition by
  • duplex TEK multistage gasifier is operated using recuperative heat recovery in an autothermal process regime, that is, there is no additional external heat energy supply in this mode.
  • the horizontally mounted on a frame pre-carburetor includes a cylindrical carburetor shell, and in which the components of the pre-carburettor are housed.
  • a centric and horizontal hollow shaft In the interior there is a centric and horizontal hollow shaft, which is moved by means of a drive unit and is fixed in the end caps of the carburetor jacket with centric bearing.
  • coiled tubing In the first third of the pre-carburetor there are coiled tubing, tightly guided on the inside of the cylindrical carburetor jacket, which are connected to the hollow shaft via holding webs.
  • a continuing spiral conveyor belt preferably with a steep angle of attack, is also connected via holding webs to the hollow shaft, beginning in the second third of the VV and ending in the first part of the third, last third VV.
  • the spiral conveyor belt is also guided close to the inside of the cylindrical Vergasermantels-VV and acts in the region of the inner radius of the carburetor jacket.
  • a conical solid blade screw placed holistically on the hollow shaft, preferably with a steep angle of attack, is located inside the tube coils and the spiral conveyor belt.
  • the conical solid blade worm expands in the third, last third VV of the pre-gasifier after the end of the spiral conveyor conical to the inner radius of the Vergasermantel- VV and is guided close to the inside of the cylindrical Vergasermantels.
  • a good entry with quick closing slide is located in cylindrical carburetor jacket in drop height above the located in the first third of the pre-carburetor tube coils.
  • An adequate Gutaustrag is arranged below the conical Vollblattschnecke in the last third of the VV.
  • a Schwelgasab placed opposite the Gutaustrag located at the top of the carburetor VV.
  • Vergasungsmittelverteiler shafts each with separate control valves in the lower part of the cylindrical Vergasermantel- VV incorporated Vergasungsstoffschlitze with deflectors.
  • the main carburetor placed vertically in a frame HV is material and flow conducting freely and pressure and gas tight and arranged without physical separation from the VV. It is directly connected to the pre-carburettor via the carbon feed and the low-pressure gas line with the Schwelgas fan.
  • the carbon transport is preferably carried out as a tube screw conveyor and preferably heated.
  • the HV includes an upper part and a lower part.
  • the upper part of the HV includes
  • the upper part of the includes the Nachreduktionsraum.
  • the upper part is locked by means of supports on the frame HV and connected via a flange with the lower part.
  • the lower part of the HV comprises
  • a centrally assigned trough worm conveyor with a perforated wall which is preferably driven by an electric motor
  • the carrier shaft is connected to a space-enclosing screw conveyor and running in the carbon tray as mixing tools.
  • the mixing tool is preferably made of ceramic and is preferably driven by means of an electric motor.
  • the upper inside of the base-HV with a sandwich mold insert preferably as a fireproof composite construction, loose or solid executed.
  • the entire lower part HV is located by a lifting / lowering device.
  • a reflector hood In the lower third of the upper part of the HV is a reflector hood, which is mounted on segment supports. As a result, partial flow channels are formed between the semicircular reflector hood and the refractory insulation.
  • the reflector hood is located in the interior of the HV between the underlying oxidation-reduction space and the above-located Nachreduktionsraum with gasification gas discharge. Lead into the oxidation-reduction space the hot gas inlets connected to the hot gas supply from the hot gas generator.
  • the carburetor and the main carburetor are identical to The carburetor and the main carburetor.
  • the heat exchanger cyclone is a double-walled and separate air and gas guided version with cyclone residue discharge.
  • the heat exchanger cyclone is gas-tightly connected to the gasification gas discharge from the main gasifier via a large capacity compensator.
  • the fresh air is supplied via a fresh air supply with a fresh air fan controlled the double-walled enclosure.
  • the cyclone hot air line directs the heated fresh air to the gasification agent mixing section.
  • the cyclone gasification gas outlet is connected via a box compensator and a connector to the main heat exchanger.
  • the main heat exchanger is preferably a gas-air or gas-oil version. Connected to the main heat exchanger are a leading to the process fan gasification gas line, a hot air supply for oxygen preheating, a hot air outlet for the external use of excess heat and also its own fresh air supply with fresh air fan.
  • the gasification-mixing section with the associated fittings, valves and valves will not be explained here. it includes
  • the oxygen preheating which is connected to the hot air supply coming from the main heat exchanger, a discharge line residual heat and
  • the gasification agent produced in the gasification agent mixing section is passed through the gasification agent line to the gasification agent heater.
  • the gasification agent stream splits into the gasification agent supply VV and the gasification agent supply HV.
  • a process fan that generates from the Guteintrag the pre-gasifier to the process fan negative pressure and promotes the gasification gas for further energetic use in the gasification gas discharge.
  • a hot gas generator For startup and shutdown of the entire system of the gas line is a hot gas generator with hot gas supply upstream of the carburetor and main carburetor.
  • duplex TEK multistage carburetor with turbulent-expansive carbon bed is preferably operated with a slight negative pressure in such a way that over the Guteintrag in Vorvergaser up to the gasification gas utilization after the main heat exchanger, an energetic conversion he follows.
  • the high-calorie carbonaceous material to be treated is presorted to the product input, fed crushed and preferably has only 10-mass% water bound.
  • the material is loosened after the entry on the Guteintrag by means of coiled tubing, which are placed in the first third VV, and conveyed on a spiral conveyor belt and a conical full leaf auger.
  • the spiral conveyor joins the coiled tubing in the second third of the VV and exits in the first part of the third, last third VV.
  • a concentric and holistic on the hollow shaft placed conical full leaf screw is located within the coiled tubing and the spiral conveyor belt and expands to the end in the third, last third VV, after the end of the spiral conveyor belt to the inner radius of the pre-gasifier.
  • the hollow shaft is mounted in the end caps with centric storage. The transport of goods from Guteintrag to Gutaustrag at the end of Vorvergasers done without superficial mixture.
  • the hollow shaft with coiled tubing, spiral conveyor belt and conical solid blade screw is set in a rotating motion by a drive unit.
  • the entry of the hot gasification agent is carried out below the material via partially arranged Vergasungsschlitze in the lower part of the cylindrical Vergasermantels-VV via the Vergasffentivverteiler shafts and is controlled by valves.
  • the estate is supplied with hot gasification agent and flows around.
  • the deflectors installed above the gasification agent slots protect the gasification agent slots from blockages.
  • the material is further promoted by the subsequently arranged spiral conveyor in the central part, which is supported by a different relative movement to the conical full leaf auger, which is based on the different pitches of spiral conveyor and conical full leaf auger.
  • the carbon transport which is preferably designed as a tube screw conveyor and heated
  • the carbon coke is transported to the main gasifier.
  • the carbonization gas forming in the pre-carburettor is conveyed via the carbonization gas discharge, which is arranged above the product discharge, via a further Schwelgastechnisch simultaneously led to the main gasifier.
  • the carbonization gas and the carbon coke are brought together and at the same time introduced without spatial and fluidic interruption in the lower part HV.
  • the forming carbon bed in the carbon sump is formed by the carbon coke that is introduced into the lower part HV via the tubular carbon entry.
  • the tubular carbon entry is in turn connected via the tube compensator with the carbon delivery of the pre-gasifier (VV) conveyor technology and is placed laterally to the carbon trough at the outer end wall.
  • VV pre-gasifier
  • a carrier shaft which is mounted centrally in the tubular carbon deposit, is preferably driven by an electric motor and is mounted counter to the opposite end wall. Within the tubular carbon entry, the carrier shaft is designed as a screw conveyor and further equipped in the carbon tray with mixing tools.
  • the trough screw conveyor opens in the discharge in a separate residue discharge with residue sluice, also disposed within the comprehensive Vergasungsstoffschachtes, this flow and pressure technology is not associated with the residue discharge.
  • the carbon sump above the carbon bed in the gasification area with a sandwich insert is refractory and heat resistant Composite construction, single or multi-layered, loose or fixed.
  • the lower part is locked in its entirety by means of lifting / lowering device on the upper part and is connected via the flange with this gas-tight, but releasably connected.
  • the upper part is designed cylindrically, above with lid and overpressure protection final, and is supported vertically by externally mounted on the cylindrical carburetor HV-bearing, which are connected to the frame HV.
  • the inner wall of the upper part is provided with a refractory insulation.
  • the interior of the upper part is divided by a placed in the lower third, semicircular and downwardly open reflector hood in an overlying Nachreduktionsraum and underlying oxidation-reduction space with hot gas inlet openings.
  • the post-reduction space and the oxidation-reduction space are connected to one another in gas and flow-conducting manner via partial flow channels.
  • the arranged above the Nachreduktionsraumes gasification gas discharge is connected by means of large capacity with the following double-walled heat exchanger cyclone.
  • the cyclone residue discharge is arranged below and the cyclone gasification gas discharge above the gasification gas entry into the heat exchanger cyclone.
  • Fresh air is supplied through the fresh air supply into the double wall of the heat exchanger cyclone and controlled by fresh air fan.
  • the heated air is supplied via the cyclone hot air line of the gasification agent mixing section.
  • the cycled (passed through the heat exchanger cyclone) gasification gas is passed through the cyclone gasification gas discharge, a box compensator and a connector in the main heat exchanger, the embodiment of which is not the subject of the invention.
  • the main heat exchanger is also fresh air over a separate and controlled fresh air supply supplied with fresh air fan.
  • the tar-free gasification gas is subsequently passed via the gasification gas line, the process fan and the gasification gas discharge to a further gas treatment, which is not the subject of the invention, and is then available for further energetic use.
  • recuperated hot air from the heat exchanger cyclone and main heat exchanger is proportionally fed to the gasification agent mixing section.
  • This consists of an oxygen feed with a controlled system oxygen, an oxygen pre-heater and an oxygen-air mixing section.
  • the gasification agent mixing section with the cyclone hot air line and hot air supply, output side connected to the gasification agent line to the gasifier heater and the discharge line residual heat to hot air discharge.
  • the externally supplied oxygen is regulated by the controlled system oxygen and heated by means of an oxygen preheater.
  • the oxygen preheating is used to preheat the admixed oxygen in the gasification agent.
  • the heated oxygen is mixed with the hot air from the heat exchanger cyclone via the oxygen-air mixing section, fed via the cyclone hot air line, and passed on via the gasification medium line to the gasification agent heater.
  • the gasification agent heater is divided into two lines by means of process-controlled valve flaps, the gasification agent feed HV to the main gasifier and the gasification agent feed VV to the pre-gasifier.
  • the gas line is a Hot gas generator, external energy supplied, upstream.
  • the duplex TEK multi-stage gasifier and the entire system technology are controlled and driven by a process control unit that is not the subject of the invention.
  • the excess hot air from the heat exchange process can be supplied via the hot air removal of an external use.
  • Gasifier heater and hot gas generator is organized a continuous and autothermal process, in which the carbonaceous material is dried, degassed and carbonized, reduced to a carbon coke and further converted to an energetically usable and combustible tar-free gasification gas. This is done by initiating thermochemical cleavage of the organic compounds by controlled addition with hot gasification agent. The gasification agent is placed over the below in the cylindrical carburetor VV
  • a centrally acting conical solid leaf auger placed holistically on the hollow shaft acts on the third, last third VV and widens towards the end of the spiral conveyor belt in the third, last third VV to the inside radius of the pre-gasifier.
  • the coiled tubing and the spiral conveyor belt are guided close to the inside of the cylindrical Vergasermantels-VV. It comes to comprehensive thermochemical chain reaction in the interior of the pre-gasifier (VV) by maintaining parallel exothermic and endothermic reactions with a vaporization of residual moisture, degassing and charring all Vergasungsgasanteile with the carbonaceous Good. This process can be supported by the admixtures via the additive entry.
  • the carbon coke as well as the resulting carbonization are subsequently, without interruption and spatial separation, mass and fluidically free as well as pressure and gas-tight, in the main gasifier (HV) passed.
  • HV main gasifier
  • the carbon coke and the carbonization are further thermochemically treated with a combined, ascending DC direct current gasification.
  • the carbon coke is transported via a carbon transport, which is preferably designed as a tube screw conveyor and preferably heated, and further via the tubular carbon entry into the carbon trough.
  • the carbon coke is flowed through the partial semicircular hole bottom with a pressure-biased hot gasification agent, preferably a Sauers toff-air mixture.
  • a pressure-biased hot gasification agent preferably a Sauers toff-air mixture.
  • AMR principle By means of the mixing tools placed in the carbon bed there is a gas, mixing and stirring (AMR principle).
  • AMR principle By means of the mixing tools placed in the carbon bed there is a gas, mixing and stirring (AMR principle).
  • AMR principle gas, mixing and stirring
  • This is accompanied by thermochemical chain reactions through permanent availability of process-related gasification agent (oxygen-air fractions) at the individual carbon particles (partial hot spots
  • the gas-residual-carbon mixture passes turbulent continuing to flow in the over-dimensioned compared to the oxidation-reduction space cylindrical Nachreduktionsraum with sufficient residence time for complete conversion of the residual Kohlenstaub- shares to a combustible tar-free gasification gas.
  • the gasification gas is passed further into the heat exchanger cyclone. There is a separation still entrained coarse residual carbon particles and a use of radiant heat on the fresh air heated in the double wall and their forwarding in the gasification agent mixing section.
  • the gasification gas is forwarded to a subsequent main heat exchanger with partial removal of the recuperated heat to the gasification agent mixing section and the predominant heat share via the hot air discharge for external use.
  • the transfer of the gasification gas is carried out by means of process fan via the gasification gas discharge overpressure technology for the energetic use of the gasification gas. If necessary, the gasification gas is passed over an additional gas treatment section, which is not the subject of the invention.
  • the total process of the process-required heated air portion is provided via the gasification agent mixing section to maintain the autothermal process control.
  • the required amount of hot air coming from the main heat exchanger via the hot air supply is combined with the oxygen to be heated.
  • the oxygen is fed via an external oxygen supply and the controlled system oxygen of the oxygen preheating.
  • the heated oxygen then enters the oxygen-air mixing section, which is supplied with hot air from the cyclone hot air line.
  • the oxygen-air mixture is over the Gasification line fed to the gasifier heater.
  • the oxygen supply is not the subject of the invention.
  • the resulting and heated gasification agent is subsequently fed via demand-controlled valve valves on the one hand via the gasification agent supply VV the pre-carburetor (VV) and the other via the gasification agent supply HV to the main gasifier (HV).
  • FIG. 2 is a schematic representation of a cross section of the duplex TEK multistage carburetor with pre-carburettor and main carburetor according to FIG. 1, FIG.
  • FIG. 3 shows a schematic partial section of the pre-gasifier according to FIG.
  • Fig. 5 a schematic partial section of the cross section according to
  • FIGS. 4 and 6 shows a side view of the duplex TEK multistage gasifier with recuperative heat utilization and production in an overall plant for the thermal decomposition of high-calorie organic wastes according to FIGS. 1 and 2
  • FIG. 7 is a plan view of the duplex TEK multistage carburetor with recuperative heat utilization and production in an overall plant for the thermal decomposition of organic wastes of high calorific value according to FIG. 1.
  • Fig. 1 shows a duplex TEK multi-stage gasifier, which consists of a Vorvergaser (1) and a main gasifier (2), with a downstream heat exchanger cyclone (61), a subsequent main heat exchanger (66), a A gasification agent mixing section (71) comprising an oxygen supply (87), a controlled system oxygen (88), an oxygen preheater (74) and an oxygen-air mixing section (89), a gasification agent heater (76), a hot gas generator ( 77) and a process fan (83), wherein these material, pressure, gas and flow-conducting, without spatial separation from each other, as well as process and control technology via a process control and regulation unit (91) are controlled, the interconnected Vorvergaser (1) and main carburetor (2) represent the core.
  • a process control and regulation unit (91) are controlled
  • a frame VV (5) placed pre-carburetor (1) comprises a horizontally oriented cylindrical Vergasermantel- VV (7) with preferably semicircular end covers with centric bearings (8) at its two ends, on and in the components of the pre-gasifier (1) are housed.
  • a goods entry (19) with a quick-closing slide (25) is located at the top at the beginning of the first third VV (84) of the pre-gasifier (1).
  • VV (9) of the pre-gasifier (1) is located, as shown in Fig. 2, via a drive unit (18) rotatably moving, centrally and horizontally aligned hollow shaft (13) in the End caps with centric bearing (8) of the cylindrical carburetor VV (7) is fixed.
  • VV (84) of the pre-gasifier (1) are coiled tubing (10), which are connected by retaining webs (12) with the hollow shaft (13) and thereby close to the inside of the cylindrical Vergasermantels -VV (7) ,
  • Vorvergaser (1) is still one of the Roh dietaryin (10) continuing spiral conveyor belt (11), preferably with steep angle, starting in the second third VV (85) and expiring in the third third VV (86) of the pre-gasifier (1 ), wherein it is also over the entire length also close to the inside of the cylindrical Vergasermantels VV (7) of the pre-gasifier (1) is guided and in the region of the inner radius of the cylindrical Vergasermantels -VV (7) acts.
  • a conical solid blade screw (14) On the hollow shaft (13) is centrally placed a conical solid blade screw (14), preferably with a steep angle of attack.
  • the diameter of the conical full-blade auger (14) lies inside the tube spiral (10) and spiral conveyor belts (11) and widens conically in the last third-VV (86) of the pre-gasifier (1) so that it is outside the area of the spiral conveyor belts (11). is guided close to the inside of the cylindrical Vergasermantels-VV (7) and there ultimately causes the Gutaustrag (20).
  • pre-gasifier (1) At the end of the pre-gasifier (1) are located at the bottom of an opening for Gutaustrag (20) and at the top of an opening for Schwelgasab arrangement (21).
  • Gas-tight gasification agent distributor shafts (15) mounted below the pre-gasifier (1) surround the gasification agent slots (16) provided with respective separate control valves (24) with baffles (17) in the lower part of the cylindrical carburetor jacket VV (7).
  • Advantageously associated with this equipment are measuring stubs (23), overpressure safeguards (22), additive inlet (26) and manholes VV (27), in each case present once or several times.
  • a frame HV (6) placed main carburetor (2) is material, pressure, gas and flow leading via a carbonization gas line (4) with a carbonization fan (28) and a carbon ( 3), the latter preferably designed as a tube screw conveyor and preferably heated, connected via a pipe compensator (37) with the pre-carburetor (1) and a total of thermally insulated.
  • the main carburetor (2) shown in FIGS. 2 and 4 comprises an upper part (29) and a lower part (31) which are connected by a flange connection (33).
  • the upper part (29) of the main carburettor (2) comprises a vertically oriented cylindrical carburetor jacket HV (39) with an upper, preferably half-round cover (30) and a lower flange connection (33).
  • An opening for the gasification gas discharge (32) is located at the upper end of the cylindrical carburetor jacket HV (39).
  • the inner walls of the cylindrical carburetor jacket HV (39) are lined with a refractory insulation (40).
  • the reflector hood (41) divides the interior of the upper part (29) into an upstream post-reduction space (43) and an oxidation-reduction space (44) located below. Between the refractory insulation (40) on the inner walls of the cylindrical Vergasermantels - HV (39) and the reflector hood (41) a plurality of partial flow channels (53) are formed, through which the process gas from the oxidation-reduction space (44) in the Nachreduktionsraum (43 ). By means of at least one hot gas inlet opening (45) in the cylindrical carburetor jacket HV (39) hot air is guided into the oxidation-reduction chamber (44) when the carburettor is started up and shut down.
  • At least one measuring port (23), at least one overpressure protection (22) and at least one manhole HV (35) are further attached.
  • a plurality of supports (34) support the top (29) by connecting it to the frame HV (6) of the main carburettor (2).
  • the reflector hood (41) is arranged so that the Nachreduktionsraum (43) and the oxidation-reduction space (44) are in a space ratio of 4 to 1 to each other.
  • the lower part (31) of the main carburettor (2) comprises a carbon trough (46) with an upper flange connection (33) to which the lower part (31) and the upper part (29) are firmly and gas-tight, but detachable.
  • the carbon trough (46) comprises a semicircular cross section, end walls (49) closing on both sides, a partial hole bottom (47) and slag deflector (59).
  • gasification agent supply (79) gasification agent in a below the carbon sump (46) mounted enclosing Vergasungsschacht (50) can be introduced, which then by the partial Hole bottom (47) and the trough screw conveyor with perforated wall (48) into the carbon trough (46) flows.
  • the carbon produced by the pre-carburetor (1) is supplied through a tubular carbon entry (36) mounted centrally on an end wall.
  • the carbonization gas coming from the pre-carburettor (1) is conducted through an end-side carbonization feed (81) via the carbonization gas line (4) with a carbonization gas fan (28) into the carbon trough (46). All moving parts are preferably driven by an electric motor (57).
  • the upper part (29) of the main carburettor (2) is connected to a frame HV (6) via several supports (34).
  • the inside of the lower part (31) of the main gasifier (2) above the support shaft (54) for high temperature and corrosion protection is provided with a sandwich mold insert (58) designed as a refractory composite construction, single or multi-layered, loose or solid is.
  • the main carburettor (2) is equipped with a lifting and lowering device (38) with which the lower part (31) can be separated from the upper part (29) for maintenance work.
  • the Vergasungsgasaustrag (32) of the main carburetor (2) is connected via a large capacity (60) with the heat exchanger cyclone (61).
  • the heat exchanger cyclone (61) is executed double-walled with a separate guidance of air and carburetor gas.
  • Fresh air supplied controlled by a fresh air evaporator (70) is conducted via a fresh air feed (69) into the heat exchanger cyclone (61).
  • the heated fresh air is supplied via the cyclone hot air line (64) of the gasification agent mixing section (71). Excess heated fresh air is available via the discharge line residual heat (75) at the hot air outlet (68) for external use.
  • the treated gasification gas is passed via the cyclone gasification gas outlet (63), a connector (82) and a box compensator (65) in the main heat exchanger (66).
  • the main heat exchanger (66) may be a gas-air or gas-oil version. Described here is a gas-air version.
  • Fresh air supplied controlled by a fresh air fan (70) is conducted via fresh air feed (69) into the main heat exchanger (66) and heated there.
  • the heated fresh air is supplied via the hot air supply (73) of the gasification agent mixing section (71).
  • hot air outlet (68) Excess heated fresh air is available for external use via hot air outlet (68).
  • the gasification gas is fed via the main heat exchanger (66), the gasification gas line (67), the process fan (83) and then via the gasification gas discharge (90) overprinted energy use.
  • the gasification agent mixing section (71) comprises a hot air feed (73), a sour material supply (87) with a controlled system oxygen (88), an oxygen pre-heater (74) and an oxygen-air mixing section (89).
  • the input side is the Gasification agent mixing section (71) with the cyclone
  • the externally supplied oxygen is controlled by the controlled system oxygen (88) and heated by means of oxygen preheating (74), which is connected to the hot air supply (73) and discharge line residual heat (75).
  • the heated oxygen is mixed with the hot air from the heat exchanger cyclone (61) via the cyclone hot air line (64) via the oxygen-air mixing section (89) and fed to the gasifier heater (76) via the gasification line (72) ).
  • the gasifier heater (76) divides by means of process-controlled valve flaps into two lines, the gasification agent feed HV (79) to the main gasifier (2) and the gasification agent supply VV (80) to the pre-gasifier (1).
  • a hot gas generator (77) is connected via a hot gas supply (78) with the Schugaseintrittsö réelle (45) of the main carburetor (2).
  • FIG. 3 and FIG. 5 show detailed details of the pre-carburettor (1) and the main carburetor (2).
  • the entire arrangement including the duplex TEK multi-stage carburetor is thermally insulated.
  • a process control unit (91) is connected to all components of the duplex TEK multi-stage carburettor and the entire plant data and current conducting.
  • the duplex TEK multistage gasifier is preferably operated with a slight negative pressure generated by the process fan (83). causing a continuous gas flow from Guteintrag (19) to the gasification gas discharge (90),
  • the high-calorie carbonaceous material to be treated is pre-sorted and comminuted ready and preferably contains a maximum of 10 mass percent water. It is fed to the pre-carburetor (1).
  • the estate is loosened by means of coiled tubing (10), which are placed in the first third VV (84), and a spiral conveyor belt (11) and a conical Full leaf auger (14) further promoted.
  • the spiral conveyor belt (11) adjoins the tube coils (10) in the second third VV (85) and exits in the first part of the third, last third VV (86).
  • the concentric and integral on the hollow shaft (13) placed conical full-blade screw (14) is located within the coiled tubing (10) and the spiral conveyor belt (11) and expands to the end in the third, last third VV (86), after the end of Spiral conveyor belt (11), to the inner radius of the cylindrical Vorvergasermantels-VV (7).
  • the hollow shaft (13) is mounted in the end caps with centric bearing (8).
  • the material transport from Guteintrag (19) for Gutaustrag (20) at the end of the pre-gasifier (1) takes place without superficial mixture.
  • the hollow shaft (13) with coiled tubing (10), spiral conveyor belt (11) and conical solid blade screw (14) is set in a rotating movement by a drive unit (18).
  • pre-gasifier (1) In the effective range of the pre-gasifier (1) are by the designated devices in order and execution, by controlled, targeted and direct admission of gasification, by specific and graded temperature zones, supported by process-promoting admixtures on the additive entry (26), locally process-oriented parallel and stable set partial endothermic and exothermic reaction zones, which are associated with a quantitative and qualitative coke formation in the conveying direction of Gutsstrom.
  • the product is treated with hot gasification agent, preferably consisting of a process-controlled and proportionately recycled oxygen-air Mixture, charged and circulated, the gasification agent supplied via the gasification agent distributor shaft (15), controlled by the valves (24) in time and quantity and introduced through the gasification agent slots (16) arranged in the lower part of the cylindrical carburetor VV (7) becomes.
  • the gasification agent slots (16) are protected by the installed deflector (17) from clogging.
  • the continuously formed carbon coke is transported via the Gutaustrag (20) through the gas-tight carbon conveyor (3), which is preferably equipped with a pipe compensator (37) to the main gasifier (2).
  • the carbonization gas forming is passed via a Schwelgasab Entry (21) arranged above the Gutaustrags (21) with a carbonization fan (28) to the main carburetor (2) in the lower part (31), where the carbonization gas through an end side Schwelgaszu operation (81) in the Carbon trough (46) is introduced.
  • the carbonization gas and the carbon coke are thus brought together in the lower part (31) without spatial and fluidic interruption.
  • the moving parts of the pre-gasifier are driven by a drive unit (18), preferably by an electric motor.
  • the carbon fed to the main gasifier (2) from the pre-carburator (1) via the carbon conveyor (3) is conveyed through the carbon feed (36) by the screw conveyor (55) into the carbon sump (46) forming a carbon bed.
  • the carbonization gas supplied by the pre-carburettor (1) via the carbonization gas line (4) is introduced into the carbon trough (46) and thus into the carbon bed by the carbonization gas feed (81) at the same time.
  • the same hot gasification agent as is supplied to the pre-carburettor (1) passes through the gasification agent shaft (50) and through the divided partial hole bottom (47) with the perforated wall trough-screw conveyor (48) arranged therebetween into the carbon trough (46).
  • the carbon bed is in the Carbon trough (46) mixed by the mixing tools (56) and stirred. It comes through the biased hot gasification agent, which is proportionally the same recycled oxygen-gas mixture as in the pre-carburetor (1), to a gas on the carbon bed and in the interaction of these factors (AMR principle / Aufgasen, mixing, stirring) a voluminous float.
  • the pressure and the amount of the supplied gasification agent is controlled so that the carbon bed is gassed and the carbon particles are enveloped by the gasification agent, called wrapping, wherein the carbon bed assumes a quasi-fluid state and the carbon thermochemically proportioned to a gasification gas.
  • the accompanying oxidation-reduction reactions lead to a thermochemical disruption of the molecular carbon compounds into gaseous constituents, to permanent flooding and thus to complete gasification and to rapid qualitative and quantitative conversion of the fluid carbon and the carbonization gases into a combustible gasification gas, in particular from CO, CO 2 , CH 4 , H 2 , H 2 O, N 2 .
  • the continuous mixing and agitation of the suspended turbulent-expansive carbon bed results in a gasification process without the formation of process-disturbing Flow channels, dead zones, bridges or slag deposits with increasing bonding of the carbon bed and therefore not to stop the entire process.
  • thermochemical loading of the gasification gas components of the carbon particles entrained upward in the flow stream from the fluid carbon bed takes place in the oxidation-reduction space (44) below the reflector hood (41) and above the suspended turbulent-expansive carbon bed by another high-temperature gasification with oxidation Reduction reactions and homogeneous secondary reactions in turbulent flow.
  • the mixture of residual carbon, residual carbonization gas, gasification gas and raw gas passes through partial flow channels (53) turbulent continued flow in the compared to the oxidation-reduction space (44) oversized cylindrical Nachreduktionsraum (43). It remains there with sufficient residence time, preferably at least for 3 seconds, for complete conversion to a tar-free combustible gasification gas leaving the main gasifier (2) via the gasification gas discharge (32).
  • the gasification gas continues to flow through the heat exchanger cyclone (61), the gasification gas being purified by separation and discharge of possibly entrained coarse residual coal dust and other particles.
  • the cycled coarse residues are discharged from the gas stream via the cyclone residue discharge (62) arranged below.
  • a first reduction in temperature of the hot gasification gas is carried out by the supplied in the cyclone double wall fresh air, the amount supplied via a fresh air supply (69) and a fresh air fan (70) controlled and after their warming over the cyclone hot air line (64) continuing the Vergasungsstoff- mixing section (71) is supplied.
  • the amount of heat gained is used to maintain autothermal process control.
  • the temperature-reduced gasification gas is supplied from the heat exchanger cyclone (61) below the main heat exchanger (66).
  • the fresh air controlled by a further fresh air fan (70) and via a further fresh air supply (69) is heated and supplied proportionally via the hot air supply (73) to the gasification agent mixing plug (71).
  • the excess warm air from the main heat exchanger (66) and from the gasification agent mixing section (71) is made available for external use directly and indirectly via the discharge line residual heat (75) via the hot air discharge (68).
  • the gasification gas is supplied from the main heat exchanger (66) via the gasification gas line (67) and by the process fan (83) for further gas use via the gasification gas discharge (90), wherein the process fan (83) Produces negative pressure, which is present in the entire duplex TEK multi-stage carburetor including the downstream components from the good entry (19) to the process fan (83).
  • the hot air discharged from the main heat exchanger (66) via the hot air supply (73) is combined with the heated oxygen.
  • the oxygen is supplied via the oxygen supply (87) and the controlled system Oxygen (88) of the oxygen preheating (74) fed.
  • the provision of oxygen is not the subject of the invention.
  • the heated oxygen of the oxygen-air mixing section (89) which is fed with hot air from the cyclone hot air line (64), and then via the gasification agent line (72) to the gasifier heater (76).
  • the resulting and heated gasification agent is subsequently fed via process-controlled valve flaps on the one hand via the Vergasungsstoff- supply VV (80) to Vorvergaser (1) and the other via the gasification agent supply HV (79) to the main gasifier (2).
  • the upstream hot gas generator (77) is only actively used during startup and shutdown to heat up and down the overall system. This ensures that the temperatures in the carburetor (1) and main carburetor (2) and the downstream components up to and including the process fan (83) have the necessary height for the thermochemical reactions. This ensures that the thermochemical reactions during start-up from the beginning with the first Guteintrag and shutting down to the end with the utilization of the last Guteintrages complete and in particular tar formation is avoided.
  • the process temperatures in the pre-carburettor (1) are preferably set and maintained in the range of 400 ° C to 600 ° C.
  • the process temperatures in the main gasifier (2) in the region of the carbon bed in the carbon trough (46) are preferably from 800 ° C to 1,200 ° C, in the region of the oxidation-reduction space (44) preferably from 1,200 ° C to 1,400 ° C and in Nachreduktionsraum (43) preferably set and maintained at 1000 ° C.
  • the gasification agent mixing section (71) with the oxygen preheating (74) is preferably operated in a temperature range of 200 ° C to 300 ° C.
  • the gasifier heater (76) is preferably operated electrically and in a temperature range of 400 ° C to 500 ° C.
  • the hot gas generator (77) is preferably operated with a fuel and in a temperature range of 850 ° C to 900 ° C.
  • Duplex TEK multi-stage carburettors and the entire plant are operated using complex process-controlled measurement and control technology.
  • duplex TEK multistage gasifier allows the continuous production of a tar-free combustible gasification gas in a stepwise autothermal process, without material, fluidic and procedural interruption, with locally determined conversion and gasification stages each with defined time, Temperature and turbulence ratios (Time-Temperature-Turbulence) and dedicated endothermic and exothermic oxidation and reduction reactions in an overall system for the thermal decomposition of an organic carbonaceous material with high calorific value without external energy supply after starting the plant by a recuperative heat utilization allows ,
  • VV 1 pre-carburettor
  • HV main carburetors

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un gazéificateur multi-étagé à lit de carbone à expansion tourbillonnaire duplex et un procédé pour faire fonctionner de manière autothermique un tel gazéificateur dans l'ensemble d'une installation pour décomposer par voie thermique un produit organique carboné en un gaz de gazéification combustible exempt de goudron. La présente invention vise à fournir un gazéificateur qui permet de pallier les inconvénients de l'état de la technique et de produire un gaz de gazéification combustibe exempt de goudron à partir d'un produit carboné. A cet effet, il est fournit un gazéificateur multi-étagé à lit de carbone à expansion tourbillonnaire duplex, composé d'un prégazéificateur (1) et d'un gazéificateur principal (2), qui est utilisé avec un cyclone d'échangeur de chaleur (61) monté en aval, un échangeur de chaleur principal (66) monté en aval, une section mélangeuse d'agents de gazéification (71), une alimentation en oxygène (87), un système régulé pour l'oxygène (88), un système de préchauffage d'oxygène (74), une section mélangeuse oxygène-air (89) ainsi qu'un système de chauffage d'agents de gazéification (76), un générateur de gaz chaud (77), un ventilateur à usage industriel (83) et une unité de commande et de régulation de processus dans l'ensemble d'une installation, par récupération de chaleur pour le processus de gazéification.
EP17808306.9A 2016-11-04 2017-10-24 Gazéificateur multi-étagé à lit de carbone à expansion tourbillonnaire duplex Pending EP3535356A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016121046.3A DE102016121046B4 (de) 2016-11-04 2016-11-04 Duplex-TEK-Mehrstufen-Vergaser
PCT/DE2017/100912 WO2018082738A1 (fr) 2016-11-04 2017-10-24 Gazéificateur multi-étagé à lit de carbone à expansion tourbillonnaire duplex

Publications (1)

Publication Number Publication Date
EP3535356A1 true EP3535356A1 (fr) 2019-09-11

Family

ID=60569531

Family Applications (1)

Application Number Title Priority Date Filing Date
EP17808306.9A Pending EP3535356A1 (fr) 2016-11-04 2017-10-24 Gazéificateur multi-étagé à lit de carbone à expansion tourbillonnaire duplex

Country Status (3)

Country Link
EP (1) EP3535356A1 (fr)
DE (1) DE102016121046B4 (fr)
WO (1) WO2018082738A1 (fr)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110484285B (zh) * 2019-08-23 2021-01-19 华中科技大学 一种聚光太阳能驱动生物质梯级利用系统
DE102020106056B3 (de) * 2020-03-05 2021-07-01 Albert Abeler Pyrolytische Gaserzeugungsvorrichtung zur Erzeugung von Synthesegas aus einem verkohlbaren Ausgangsstoff
CN115197753A (zh) * 2021-04-11 2022-10-18 江苏华威机械制造有限公司 多个气化炉集中供气的控制方法
EP4144822A1 (fr) * 2021-09-01 2023-03-08 Isomorph S.r.l. Carburateur et réacteur de gazéification avec plusieurs zones de réaction combinées
CN113958954B (zh) * 2021-11-16 2024-04-16 沈阳航空航天大学 一种多源有机固废分级燃烧/气化多功能实验炉

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2520754A1 (de) * 1975-05-09 1976-11-18 Lampl Helma Verfahren und vorrichtung zur pyrolyse von abfallprodukten
AU5856494A (en) 1993-02-02 1994-08-29 Helmut Juch Continuous degasification and/or gasification of a solid fuel or waste material
DE19937521A1 (de) 1999-08-03 2001-02-15 Harald Martin Verfahren und Vorrichtung zum Trocknen, Trennen, Klassieren und Zersetzen von Abprodukten
DE19937524A1 (de) 1999-08-03 2001-02-15 Harald Martin Verfahren und Vorrichtung zum Beseitigen von Abprodukten und Abfallstoffen
WO2001051591A1 (fr) 2000-01-10 2001-07-19 Fuerst Adrian Dispositif et procede pour produire des gaz combustibles
DE60117347T2 (de) * 2001-08-31 2006-10-12 Andrew Diss Webster Schneckenreaktor zur Vergasung
DE102008027858A1 (de) 2008-06-11 2009-12-17 Jörg HO Verfahren und Vorrichtung zur Erzeugung eines teerfreien Brenngases
DE102008058602B4 (de) 2008-11-20 2010-09-23 Eurotherm Technologies Ag Vorrichtung in Form eines Bewegt-Bett-Vergasers und Verfahren zum Betreiben eines solchen in einer Anordnung zur thermischen Zersetzung von Abprodukten und Abfallstoffen
DE202009010830U1 (de) 2009-02-05 2010-02-11 Eurotherm Technologies Ag Vorrichtung in Form eines Thermolysereaktors
WO2013068052A1 (fr) * 2011-11-09 2013-05-16 Siemens Aktiengesellschaft Procédé et système pour la production d'un gaz pauvre de gazogène
DE102012024204B4 (de) 2012-12-04 2018-02-01 HS TechTransfer UG (haftungsbeschränkt) & Co. KG Vorrichtung in Form eines Thermolyse-Rotations-Reaktors und Verfahren zum Betreiben eines solchen in einer Anordnung zur thermischen Zersetzung von Abprodukten und Abfällen
DE102013015920B4 (de) 2013-09-20 2015-12-17 Recom Patent & License Gmbh Vorrichtung in Form eines 3-Zonen-Vergasers und Verfahren zum Betreiben eines solchen Vergasers zur thermischen Umwandlung von Abprodukten und Abfällen

Also Published As

Publication number Publication date
WO2018082738A1 (fr) 2018-05-11
DE102016121046A1 (de) 2018-05-09
DE102016121046B4 (de) 2018-08-02

Similar Documents

Publication Publication Date Title
DE102016121046B4 (de) Duplex-TEK-Mehrstufen-Vergaser
EP0309387B1 (fr) Procédé et appareil pour la production de gaz de gazogène et de charbon actif à partir de combustibles solides
EP3230412B1 (fr) Gazéificateur à co-courant au lit fixé pour produire du gaz à partir des particules de biomasse
DE3335544A1 (de) Reaktorvorrichtung zur erzeugung von generatorgas aus brennbaren abfallprodukten
CH615215A5 (fr)
EP2563881B1 (fr) Procédé pour la gazéification de la biomasse
DE60033782T2 (de) Verfahren zur vergasung von kohlenstoffhaltigen treibstoffen in einem festbettvergaser
WO2010057458A2 (fr) Dispositif en forme de gazéificateur à lit mobile et procédé pour faire fonctionner celui-ci dans un système de décomposition thermique de résidus et de déchets
EP2356200B1 (fr) Procédé pour la gazéification thermochimique de combustibles solides
DD202176A5 (de) Verfahren und einrichtung zur kontinuierlichen erzeugung von brenngas aus organischen abfallstoffen
WO2011006789A2 (fr) Réacteur et procédé de gazéification de biomasse
DE102013015920B4 (de) Vorrichtung in Form eines 3-Zonen-Vergasers und Verfahren zum Betreiben eines solchen Vergasers zur thermischen Umwandlung von Abprodukten und Abfällen
DE202016106184U1 (de) Duplex-TEK-Mehrstufen-Vergaser
EP1323809B1 (fr) Réacteur à lit descendant à co-courant
EP3214155B1 (fr) Procédé pour la production de gaz de synthèse pour la combustion dans un moteur à combustion interne.
CH283414A (de) Verfahren und Vorrichtung zur Durchführung von Prozessen, bei welchen fein verteilte feste Stoffe mit Gasen in Berührung gebracht werden.
DE69204948T2 (de) Methode und Vorrichtung zum Vergasen von festen Brennstoffen, enthaltend schmelzbare nicht-brennbare Materien.
EP2705121B1 (fr) Procédé et dispositif pour l'élaboration de gaz de synthèse à partir de substances de départ carbonées, par gazéification dans un réacteur à courant tourbillonnaire
EP0126408A2 (fr) Convertisseur de gaz
EP1338847B1 (fr) Réacteur vertical à cocourant
DE102006058673A1 (de) Vorrichtung und Verfahren zur Schwachgaserzeugung aus organischen Energieträgern
DE202009010833U1 (de) Anordnung zur Aufbereitung und thermischen Behandlung von Abprodukten und Abfällen
WO2011003374A2 (fr) Ensemble et procédé pour la préparation et le traitement thermique de résidus et de déchets, et procédé permettant de faire fonctionner ledit ensemble (procédé de fission-thermolyse)
DE8328140U1 (de) Reaktorvorrichtung zur Erzeugung von Generatorgas aus brennbaren Abfallprodukten
EP1945741B1 (fr) Procede et dispositif pour obtenir de l'energie a partir de supports bioenergetiques et d'autres matieres organiques

Legal Events

Date Code Title Description
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: UNKNOWN

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE

PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20190523

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAV Request for validation of the european patent (deleted)
DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20200825

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS