EP2016159A2 - Gazéificateur de biomasse et procédé de gazéification allothermique de biomasse - Google Patents

Gazéificateur de biomasse et procédé de gazéification allothermique de biomasse

Info

Publication number
EP2016159A2
EP2016159A2 EP07722278A EP07722278A EP2016159A2 EP 2016159 A2 EP2016159 A2 EP 2016159A2 EP 07722278 A EP07722278 A EP 07722278A EP 07722278 A EP07722278 A EP 07722278A EP 2016159 A2 EP2016159 A2 EP 2016159A2
Authority
EP
European Patent Office
Prior art keywords
reactor
biomass
biomass gasifier
gasifier according
gas
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.)
Granted
Application number
EP07722278A
Other languages
German (de)
English (en)
Other versions
EP2016159B8 (fr
EP2016159B1 (fr
Inventor
Dieter Schillingmann
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.)
Rew Regenerative Energie Wirtschaftssysteme GmbH
Schillingmann Dieter
Original Assignee
REW Regenerative Energie Wirtschaftssysteme GmbH
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 REW Regenerative Energie Wirtschaftssysteme GmbH filed Critical REW Regenerative Energie Wirtschaftssysteme GmbH
Publication of EP2016159A2 publication Critical patent/EP2016159A2/fr
Application granted granted Critical
Publication of EP2016159B1 publication Critical patent/EP2016159B1/fr
Publication of EP2016159B8 publication Critical patent/EP2016159B8/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • C10J3/02—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
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C10J2200/158—Screws
    • 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1253—Heating the gasifier by injecting hot gas

Definitions

  • the present invention relates to a biomass gasifier for pyrolysis and gasification of biomass for producing a fuel gas or fuel gas mixture and a method for obtaining such fuel gases.
  • Biomass gasifiers are known as such.
  • EP 1447438 A1 e.g. an apparatus for pyrolysis and gasification of biomass known.
  • the biomass to be gasified is dried in the prereactor and pre-pyrolyzed and then reaches the main reactor.
  • the masses to be gasified are further pyrolyzed and partially gasified, then the solids are discharged and the gases are fed to a secondary reactor.
  • the gas is passed through a continuous filter in which it is to be cleaned and cooled.
  • Pre-reactor, main reactor and post-reactor are heated exclusively from the outside.
  • the present invention is based on the object to provide a biomass gasifier, which achieves both a higher conversion through gasification, as well as a comparatively clean fuel gas with high hydrogen and / or carbon monoxide - share and with only minor impurities, especially tar , which may even be used without further purification of gas by reactors or scrubbers, for example in an internal combustion engine, Stirling engine, a gas turbine or fuel cell (in particular after removal of the non-water substance fraction).
  • the subject of the process according to the invention is a pyrolytic, allothermal gasification.
  • Characteristics of the present invention is a stepped conversion into a plant with pre-reactor and main reactor and secondary reactor.
  • Biomass in the sense of the present invention are i.a. biogenic and animal by-products or industrial by-products or by-products from biogenic sources.
  • the process is suitable for moist biomass, with water contained in the biomass representing the gasification agent used in the main reactor and, if the biomass is sufficiently moist, no further gasification agent has to be added.
  • the available fuel gas is better suited for use in combustion in heat engines, as the comparable known method, in addition, the product of the process is a solid carbonaceous residue, which is suitable as a high quality fuel.
  • a biomass gasifier designed according to the invention has the advantage that the gas is discharged together with the solid in a temperature-controlled delivery line. It has proven to be advantageous if the discharge line is filled over the entire cross section with the solid bed and thus the gas must flow through this bed. Due to the intense gas-solid contact at high temperatures in this discharge the secondary degradation of the higher hydrocarbons, especially tars. For the purposes of the invention, this discharge line constitutes the secondary reactor.
  • the procedure according to the invention has the advantage that the outlay on equipment for producing an economically usable product gas can be kept low.
  • the pre-reactor has the function of compressing biomass, heating it and, if necessary, extracting water up to a defined moisture content.
  • Oxygen deficiency means that insufficient oxygen is provided compared to the amount that would be required to oxidize the carbon to CO 2 , so that the reaction with respect to the carbon is essentially led to CO.
  • the main reactor of the biomass gasifier has one or more elongated heating elements in the core (s) of the transport screw (s) which, in addition to the heating from outside, heat / heat the interior of the main reactor without any replacement of the heat transfer medium with the interior of the main reactor takes place, ie the heat transfer takes place through the walls of the soul into the interior of the reactor.
  • the secondary reactor and / or the prereactor may also have such heating elements in the core (s) of the screw conveyor (s), in particular for the secondary reactor because higher temperatures are required than in the prereactor.
  • the screw conveyor of the main reactor has a mixing and conveying function and can be designed in the form of a spiral conveyor.
  • the prereactor preferably has a twin screw and possibly one or two elongate heating elements in the souls of the twin screw.
  • the gas solid contact is significantly increased, so that the gasification can be done better and more intense.
  • the degree of filling of the main reactor can be influenced so that adjusts a backwater at the end of the main reactor and can be set at least in the secondary reactor, a fully filled cross-section that the gas there must flow through the entire solid surface of the gas, which positively influences both the gasification reactions and the secondary degradation.
  • the secondary reactor does not necessarily have to be a reactor separate from the main reactor, but the main reactor and secondary reactor can also be two zones of a reactor.
  • the secondary reactor (or in this sense equivalent to the secondary reactor zone) has a higher degree of filling (preferably 100 vol.%) Than the main reactor (or the main reactor reactor zone), wherein the main reactor is always first passed through by the filling material.
  • the advantage of the high degree of filling in the secondary reactor is: a.
  • the high degree of filling reduces the tar content in the synthesis gas, as it flows through the gas through the full amount of hot coke.
  • b. The gasification works more completely, because • the heat transfer of the allothermal gasification is better with a high degree of filling,
  • the pyrolysis / gasification of the biomass in the biomass gasifier according to the invention proceeds as follows:
  • biomass gasifier all renewable raw materials, biogenic residues and waste materials and mixtures thereof and with these - in the context of the present invention also generally referred to as biomass - are gasified, as long as they are present in a pourable form.
  • the state eg the moisture or particle size distribution of the biomass, does not matter, because the biomass gasifier can also gasify moist and inhomogeneous substances very well and economically. It is also possible to mix biomass with other non-biogenic substances. These may be, for example, household waste, sludges or other reactive carbonaceous materials.
  • contamination of the biomass with non-reactive material is up to a fraction of 20% by weight, preferably 5% by weight, harmless to gasification, if they occur in a piece that is not critical for the conveyors (screws), since these materials are discharged again after the gasification of the actual biomass.
  • non-reactive material such as metals
  • an admixture of up to 40% by weight, preferably up to 10% by weight, of fuels which are not renewable raw materials is possible, and that the biomass gasifier can nevertheless be operated economically.
  • substances or mixtures of various substances may be used as fuel, which may not be suitable as fuel in autothermal or allothermal gasifiers according to the prior art and in combustion plants.
  • the bulk material biomass is stored in a bunker, silo or storage tank and heated by the residual energy in the flue gas.
  • the pre-heated biomass is passed through a lock and conveyor in a pre-reactor.
  • the prereactor preferably takes place drying, degassing and pyrolysis.
  • the prereactor for example, is heated to temperatures of 200 0 C to 700 0 C, in particular 200 ° C to 400 ° C or 200 0 C to 300 0 C.
  • the hot gas emerging from the main reactor jacket is advantageously used with, for example, 700 to 500 ° C. as the heating medium.
  • the heating gas can be the flue gas of the downstream process of the combustion of the pyrolysis coke.
  • the prereactor preferably has a multi-shaft conveying and mixing plant, in particular designed as a twin screw, in order to enter the biomass and in particular to avoid caking problems.
  • the prereactor is designed in particular as a positive-conveying externally heated twin screw.
  • the forced delivery has the advantage that especially complex, moist to muddy biomass is easily dried in the prereactor to a defined residual moisture and pyrolyzed at the same time and thus for the supply of a solid (pyrolysis) and gas (pyrolysis gas, which at high temperature, the pyrolysis contains) serves the main reactor.
  • a twin screw or generally multi-shaft screws are screws which rotate about several axes, with the screw wings interlocking.
  • the gas leaving the prereactor is a pyrolysis gas (essentially hydrogen-free), which also contains pyrolysis oil due to the high temperatures.
  • the prereactor always has lower temperatures than the main reactor and the secondary reactor and is preferably heated by the residual heat of the main reactor.
  • the main reactor is heated by a heating device, so that in the main reactor a hot reaction zone is formed, in which temperatures of 700 ° to 950 ° C, in particular 800 to less than 900 0 C, preferably about 825 ° C prevail.
  • a heating device in which temperatures of 700 ° to 950 ° C, in particular 800 to less than 900 0 C, preferably about 825 ° C prevail.
  • In the main reactor is a driven by a motor and heated from the inside by an additional heating transport and mixing screw, which transports the fuel axially through the main reactor and mixes it.
  • the reaction in the main reactor is an allothermal gasification in the presence of water vapor.
  • the heat is supplied from the outside, wherein either a heat transfer through the reactor walls takes place and / or heat is introduced via radiation.
  • Hot gases are not conducted into the reaction space of the main reactor, at least not in the sense that supplied gases have a temperature equal to or higher than the feed of the main reactor.
  • the gases containing or consisting of oxygen in this case are not hot gases but a reaction gas.
  • the main reactor is externally heated by hot flue gases.
  • the reaction takes place in the form of an all-thermal steam reforming, in which case the residual moisture of the biomass to be gasified is preferably introduced from the prereactor as gasification agent, but if necessary, water can also be added.
  • the synthesis gas recovered in the main reactor and secondary reactor has a high hydrogen content of e.g. up to 50 vol.% (based on the gas) on or above.
  • main and secondary reactor may also include other energy input method additionally be used, such as microwaves, plasma, induction, or internal heat transfer materials, which are externally heated and internally used in the reactor for heat dissipation, for example, CaO from the main reactor CaCO 3 after CO 2 uptake is.
  • energy input method such as microwaves, plasma, induction, or internal heat transfer materials, which are externally heated and internally used in the reactor for heat dissipation, for example, CaO from the main reactor CaCO 3 after CO 2 uptake is.
  • main reactor further pyrolysis of the partially converted biomass from the prereactor takes place, in which various gaseous and condensable substances and a solid pyrolysate consisting essentially of carbon form. This takes place in the main reactor without the addition of air or oxygen.
  • the gasification of the pyrolysate with water (steam) takes place from the drying and pyrolysis of the fuel and with carbon dioxide from the pyrolysis of the fuel.
  • the main reactor is so named because here the main reaction takes place according to the purpose of the decay, namely full pyrolysis and primary gasification (proportionate generation of the highest amount of hydrogen).
  • the registered in the main reactor solid contains pyrolysis and ash, which arises in the prereactor at temperatures of 200 0 C to 700 0 C in addition to pyrolysis and pyrolysis.
  • the main reactor has a jacket, suitably with Bankgas Equipmentsblechen in the jacket.
  • heating gas e.g. hot flue gas from the plant, fed in distributed over the reactor.
  • heating acts in the soul of the screw arranged "hot pipe", which is also charged with fuel gas.
  • the solid located in the main reactor can be referred to as Pyrolysat thoroughlyung and contains ash and coke.
  • the blades of the screw are designed such that they have scoops with scoop edges arranged parallel to the reactor wall in order to pick up the wall-close solid and to convey it upwards, where the scoop empties again.
  • Gasification agent which is fed into the main reactor is primarily superheated steam and preferably originates from the prereactor or from the biomass which is introduced from the prereactor into the main reactor.
  • a separate supply of air or oxygen in the main reactor is undesirable.
  • Typical for the reaction in the main reactor is a lack of oxygen so that substoichiometric combustion of the carbon monoxide or by allothermal steam reforming hydrogen is formed.
  • At the main reactor is followed at 600 to 950 ° C, preferably 800 0 C to 850 ° C, tempered secondary reactor, by means of a conveying device, for. B. a screw conveyor, the residual coal dust with a degree of filling of 80 to 100 vol.%, Preferably 100 vol.% (At least towards the end), is transported. The gas flows through the full filling
  • Main and secondary reactors may be zones of a reactor in that the main reactor faces the prereactor and the portion of the secondary reactor adjoining the main reactor is e.g. both are part of a tubular reactor, the secondary reactor being different from the main reactor by its degree of filling.
  • the main reactor has on average fill levels of preferably less than 80% by volume, while the secondary reactor has an average fill level of 80% by volume to 100% by volume, preferably at least at the end of the secondary reactor 100% by volume.
  • the increasing degree of filling in the secondary reactor or along the main reactor can be effected by gravity (tilting of the reactor tube), geometry (reduction of the reaction space) and / or by conveying angle of the screw.
  • the gas is forced to traverse the solid, whereby an optimal amount of gas and optimum gas quality can be achieved.
  • the secondary reactor can be added as gasification agent air (or hot air), water (or superheated steam) or even pure oxygen or their mixture, preferably at the end of the secondary reactor.
  • gasification agent air or hot air
  • water or superheated steam
  • pure oxygen or their mixture, preferably at the end of the secondary reactor.
  • a lack of oxygen is preferred and more typical of the reaction in the secondary reactor, so that carbon monoxide is formed by the bottom stoichiometric combustion of the carbon.
  • the outlet of the hydrogen and / or carbon monoxide rich gas is at the end of the secondary reactor or subsequent to the secondary reactor. Gas and solid can be passed together from the secondary reactor. Subsequently, gas and solid are separated and fed to their further use.
  • the solid is in powder form and can be used by combustion for hot gas production.
  • it is advantageous that the plant is operated so that the solid powder still contains carbon to have a certain calorific value for hot gas production.
  • the secondary reactor Due to the fact that the secondary reactor is tempered, secondary degradation of the longer chain hydrocarbons, e.g. Tar, the product gas within the secondary reactor, so that the finished product gas has almost no impurities and very little tar.
  • This product gas can be used after filtering without further treatment in reactors or scrubbers, for example in an internal combustion engine, to generate electricity.
  • the discharged residue may optionally be used to operate the heater. Alternatively, or if there is an excess, the residue can be used economically as fuel or valuable material.
  • escaping gas and solid are separated.
  • the gas is then fed to a hot gas dedusting and the coal dust and ash are made available for Schugasher too.
  • the hot air can be produced.
  • the plant can even be adjusted so that there is always a sufficient amount of residual coke discharged from the secondary reactor solid, which can be used for external heating of the main and secondary reactor via the heating gas.
  • a heat transfer material can be used. If CaO is used, it is heated, for example, by the combustion process, which is maintained with discharged biocoke or pyrolysis coke from the plant, and introduced into the main reactor or possibly also via the prereactor.
  • biomass gasifier according to the invention is further exemplified by the attached figures. Show it:
  • Figure 1 is a diagram of the reaction
  • Figure 2 shows the schematic structure of the reactor.
  • Fig. 1 shows the material flow and the heating currents.
  • the bulk material biomass is stored in a bunker, silo or storage tank and heated by the residual energy of the heating gas.
  • the biomass is metered into the prereactor (1) via a lock, where it is heated by the heating current from the main reactor to the pyrolysis temperatures.
  • the partially pyrolized biomass is carried by a twin screw not shown in the main reactor, where it is further heated for the purpose of allothermic gasification.
  • the heating gas generated by combustion of coal dust or pyrolysis coke, is passed into the heating jacket of the main reactor, the main reactor and the secondary reactor exchanging with heating gas and the heating gas being used cooled to heat the pre-reactor.
  • the product gases (synthesis gas) are passed through a hot gas filter and are taken from the secondary reactor.
  • the main reactor (2) and the secondary reactor (3) is detailed.
  • the dried and partially pyrolized biomass is metered into the main reactor (2) via a shaft.
  • the main reactor is provided with a transport screw (4), which is interspersed in the soul with a hot pipe (5). If necessary, the hot pipe extends as far as the secondary reactor over the length of the tubular reactor.
  • the screw conveys the gasification product and compresses it towards the end of the main reactor.
  • Main reactor and secondary reactor are part of a tubular reactor and surrounded by a heating jacket.
  • the hotpipe is designed as a lance.
  • the heating gas (6) is introduced in the middle, bounces against the end of the lance (hottest point along the hot pipe) and is discharged internally outward along the inner surface of the lance. Via a rotary valve (7) can be metered into the secondary reactor gasification agent (water vapor, oxygen and / or air) to cause in the secondary reactor, if desired, a partial autothermal oxidation by the presence of oxygen.
  • the secondary reactor has over at least half of the conveyor line to a degree of filling of about 100%.
  • the entry and discharge from the tube reactor are marked with black arrows. Gray arrows indicate the heating gas flows (6) again.
  • Main reactor and secondary reactor have a different temperature profile, but surrounded by a common heating jacket (8).

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)
  • Treatment Of Sludge (AREA)

Abstract

Gazéificateur de biomasse pour la pyrolyse et / ou la gazéification partielle de biomasse pour la production d'un gaz combustible ou plus précisément d'un mélange de gaz combustibles. Ledit gazéificateur comprend un préréacteur, un réacteur principal chauffé par l'intérieur et par l'extérieur et pourvu d'une vis sans fin transporteuse, et un réacteur secondaire. La présente invention concerne également un procédé de traitement de biomasse dans un gazéificateur de biomasse de ce type.
EP07722278.4A 2006-04-24 2007-04-24 Gazéificateur de biomasse et procédé de gazéification allothermique de biomasse Active EP2016159B8 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE200610019452 DE102006019452B4 (de) 2006-04-24 2006-04-24 Biomassevergaser
PCT/DE2007/000720 WO2007121733A2 (fr) 2006-04-24 2007-04-24 Gazéificateur de biomasse et procédé de gazéification allothermique de biomasse

Publications (3)

Publication Number Publication Date
EP2016159A2 true EP2016159A2 (fr) 2009-01-21
EP2016159B1 EP2016159B1 (fr) 2016-05-11
EP2016159B8 EP2016159B8 (fr) 2017-03-01

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP07722278.4A Active EP2016159B8 (fr) 2006-04-24 2007-04-24 Gazéificateur de biomasse et procédé de gazéification allothermique de biomasse

Country Status (3)

Country Link
EP (1) EP2016159B8 (fr)
DE (1) DE102006019452B4 (fr)
WO (1) WO2007121733A2 (fr)

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Also Published As

Publication number Publication date
WO2007121733A2 (fr) 2007-11-01
EP2016159B8 (fr) 2017-03-01
EP2016159B1 (fr) 2016-05-11
WO2007121733A8 (fr) 2008-01-17
WO2007121733A3 (fr) 2007-12-06
DE102006019452B4 (de) 2008-05-08
DE102006019452A1 (de) 2007-10-25

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