WO2011067130A1 - Installation pour la production d'un gaz de produit à partir de matières premières organiques - Google Patents

Installation pour la production d'un gaz de produit à partir de matières premières organiques Download PDF

Info

Publication number
WO2011067130A1
WO2011067130A1 PCT/EP2010/067915 EP2010067915W WO2011067130A1 WO 2011067130 A1 WO2011067130 A1 WO 2011067130A1 EP 2010067915 W EP2010067915 W EP 2010067915W WO 2011067130 A1 WO2011067130 A1 WO 2011067130A1
Authority
WO
WIPO (PCT)
Prior art keywords
pyrolysis
gas
reactor
gasification reactor
gasification
Prior art date
Application number
PCT/EP2010/067915
Other languages
German (de)
English (en)
Inventor
Daniel Holzheimer
Original Assignee
Burkhardt 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 Burkhardt Gmbh filed Critical Burkhardt Gmbh
Publication of WO2011067130A1 publication Critical patent/WO2011067130A1/fr

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
    • C10J3/58—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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/008—Reducing the tar content by cracking
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • 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
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the present invention relates to a plant for producing a product gas from organic feedstocks with a low ash melting point.
  • the plant comprises a pyrolysis reactor for drying and pyrolysis of the organic feedstock, which has an outlet for a tar-containing pyrolysis gas and a discharge opening for a carbonaceous pyrolysis, and a downstream cracking unit for cracking the tars contained in the pyrolysis gas.
  • the invention relates to a corresponding method for producing a product gas from organic feedstocks with a low ash melting point.
  • organic feedstocks can be gasified in gasification reactors with the addition of a gasification agent.
  • a gasification agent for this purpose fluidized bed gasifier, fixed bed gasifier in countercurrent and DC gasification and multi-stage carburetor and other special forms are known.
  • the aim here is always an almost complete implementation of the carbon contained in the biomass in order to achieve the highest possible efficiency. Due to the comparatively high operating temperatures, the said gasification processes are only suitable for feedstocks with a high ash melting point, since damage to the gasifier due to slagging occurs at low ash melting points.
  • a product gas loaded with a more or less high tar content is always produced, so that as a rule gas purification after gasification is required.
  • Feedstocks with a low ash melting point are therefore usually converted into a product gas by fermentation in biogas plants.
  • this process is again not suitable for the conversion of lignin aisler feedstocks.
  • DE 199 45 771 C1 describes a multi-stage process for producing a product gas from biomass, in which the pyrolysis of the biomass and the formation of the product gas is carried out in separate reactors.
  • a first stage pyrolysis gas and coke are produced by pyrolysis.
  • the pyrolysis gas is passed into a second reactor, in which it is reacted with the aid of an inert heat carrier with the addition of a reagent, for example steam, to a product gas having a high calorific value.
  • the pyrolysis coke is discharged from the pyrolysis reactor and burned, the combustion process via the heat transfer heat for pyrolysis and for the reforming of the pyrolysis gas to the product gas supplies.
  • the heat transfer medium is in the circuit between the reforming stage and the pyrolysis reactor.
  • the object of the present invention is therefore to propose a system and a method which, with simple system technology, the generation enable a low-tarry product gas and are suitable for a variety of materials.
  • a tar-containing pyrolysis gas and carbon-containing pyrolysis coke are produced in a pyrolysis reactor from the organic feedstock.
  • the organic feedstock has a low ash melting point.
  • melting temperatures below 1.000 ° C. are understood to mean a low ash melting point, while melting temperatures above 1.000.degree. C. are to be understood as meaning a high ash melting point.
  • the ash melting points of organic feedstocks are only in the range of 700 ° C.
  • the pyrolysis gas and the pyrolysis coke are treated separately from each other.
  • the pyrolysis gas which is relatively heavily tar-charged due to the low temperatures of the pyrolysis process, is subsequently passed into a downstream cracking unit in order to crack the tars contained in it.
  • the tar-containing pyrolysis gas for gas purification or cracking of the tars is passed into a gasification reactor, in which a second organic feedstock is reacted with a high ash melting point to a low-tarry gas.
  • the tars are cracked on a glowing carbon bed of the second feed so that highly tar-charged pyrolysis gas in the gasification reactor is converted to a tarry product gas.
  • a plant for producing a product gas from organic feedstocks with a low ash melting point has a pyrolysis reactor and a downstream cracking unit, which is designed as a gasification reactor.
  • the pyrolysis reactor has an outlet for the tar-containing pyrolysis gas and a discharge opening for carbonaceous pyrolysis.
  • the gasification reactor has an inlet for the pyrolysis gas as well an outlet for the tarerarme product gas.
  • the gasification reactor is in this case designed such that the second organic feedstock is converted to a low-tarry gas and at the same time the tars of the pyrolysis gas are cracked on the glowing carbon bed of the gasification reactor.
  • the glowing carbon bed is a kind of catalyst for the cracking of the tars, so that a good decomposition of the tars is achieved.
  • This makes it possible to gasify all organic feedstocks regardless of their ash melting point by pyrolysis.
  • the product gas produced in the system according to the invention can be fed directly to a gas engine without further purification of the gas or utilized in another way. Problems due to slag formation can still be avoided by the separate further utilization of the pyrolysis gas.
  • a good efficiency of the plant is achieved because the gasification reactor produces as a cracking additional low-tarred gas, which is usable as product gas.
  • the gasification reactor is preferably designed as a DC gasifier with increasing gasification, wherein in the DC gasifier in addition a stationary fluidized bed is formed.
  • a gasification reactor is described in the patent application DE 10 2008 043 131 of the Applicant, to which reference is made in its entirety. Due to the design of the gasification reactor and the process control, a long residence time of the pyrolysis gas and a good contact of the pyrolysis with the glowing second feed can be achieved while tar suppression be prevented, so that the pyrolysis gas can be converted to a nearly tar-free product gas.
  • the second feedstock in the gasification reactor is largely completely gasified, since the gasification reactor can be made structurally simple. Discharge facilities for remaining pyrolysis residues are not required. Emerging ash can be discharged with the product gas and then in a be deposited further deposition or remain in the product gas due to the low flow rate of the second feedstock or the small amount of ash.
  • the gasification reactor has an inlet for the pyrolysis gas above its pyrolysis zone.
  • the tar-charged pyrolysis gas can thereby be introduced directly into the hot zone of the gasification reactor, so that the complete decomposition of the tars is further supported. It is particularly advantageous if the pyrolysis gas is fed to the gasification reactor in the region of the oxidation zone and thus in the hottest region. However, it is also possible, depending on the design of the gasification reactor and process control, that the inlet for the pyrolysis gas is arranged elsewhere.
  • the gasification reactor further has a feed for water or steam in the region of the reduction zone.
  • the water gas reaction in the gasification reactor can thereby be enhanced so that the decomposition of the tars is further promoted and the reduction of the oxidation products from the gasification reactor is favorably influenced.
  • the plant according to the invention comprises a separator for the ash between the pyrolysis reactor and the gasification reactor.
  • a separator for the ash between the pyrolysis reactor and the gasification reactor it may also be possible to dispense with ash deposition.
  • the pyrolysis reactor can be structurally particularly simple if it is designed as a preferably vertically arranged pyrolysis tube.
  • the promotion of the organic feedstock by the pyrolysis reactor can be done in the simplest case gravity driven.
  • a conveying device for the starting material is arranged in the pyrolysis reactor, so that the starting material can be specifically conveyed at an adjustable speed and can be discharged at the same time by means of the conveying unit.
  • the outlet for the pyrolysis gas and the outlet opening for the pyrolysis coke are separated from one another, so that a separation of the liquid and solid pyrolysis products can already take place in the pyrolysis reactor.
  • the outlet for the product gas is arranged in an upper region of the pyrolysis reactor and the outlet opening for the pyrolysis coke in a lower region, so that solid and gaseous pyrolysis products are almost automatically separated by gravity.
  • the pyrolysis reactor has a heating jacket, which can be flowed through by the hot product gas from the gasification reactor.
  • the hot product gas is preferably supplied to the heating mantle in countercurrent to the feedstock.
  • the hot product gas from the gasification reactor can be cooled, so that further cooling means for the product gas are not required.
  • the energy supply required for the pyrolysis process in the pyrolysis reactor can hereby be accomplished. It is particularly advantageous in this case if the pyrolysis process is triggered and / or maintained exclusively by the waste heat of the product gas from the gasification reactor.
  • the gasification reactor is dimensioned according to the amount of product gas producible in the pyrolysis reactor.
  • the power of the gasification reactor and / or the amount of the second feedstock to the amount of the product gas generated in the pyrolysis reactor is tuned. The consumption of the more expensive feedstock with the high ash melting point can thereby be reduced to a minimum, yet an almost complete decomposition of the tars of the pyrolysis gas can be achieved.
  • the first and / or the second feedstock are fed to the pyrolysis reactor or the gasification reactor in pelletized form. If the first organic feedstock is in pelletized form, it can be discharged again from the pyrolysis reactor in a particularly simple manner and further utilized.
  • the gasification reactor can be operated particularly favorably with wood pellets, since a uniform loosening and mixing of the fuel can take place.
  • Figure 1 is a schematic overview of the system according to the invention and of the method according to the invention for producing a product gas.
  • FIG. 1 shows a schematic representation of the system 1 according to the invention for producing a product gas 6 and a schematic representation of the process flow.
  • the plant 1 for producing a product gas 6 comprises a pyrolysis reactor 2 for drying and pyrolysis of an organic product. see feedstock 3 and a gasification reactor 4, which according to the invention forms a cracking unit for purifying the pyrolysis gas 5 produced in the pyrolysis reactor 2.
  • the plant 1 according to the invention for producing a product gas 6 uses the temperature and the carbon bed 7 of a gasification reactor 4, which in the present case is designed as a wood gasifier, in order to crack the tars of the pyrolysis gas 5 therein.
  • the present invention has now found that a gas purification of the pyrolysis gas 5 or a decomposition of the tars produced by means of a gasification reactor 4 is possible. While prior art gasification reactors themselves struggle with the tar content of the gases produced, a gasification reactor 4 can surprisingly be used as a cracking unit for tars of another process if a longer residence time of the pyrolysis gas 5 in the gasification reactor 4 is achieved and tar slippage is prevented.
  • the carbon bed 7 of the gasification reactor 4 in this case acts as a catalyst, so that with a longer residence time of the pyrolysis gas and good contact with the carbon cloth bed 7 already at Radiotem- temperature of the gasification reactor 4, a splitting of the long-chain molecules takes place.
  • wood is preferably used, as this has an ash melting point of about 1 .200 ° C.
  • the gasification reactor 4 is designed according to the present illustration as a direct current gasifier with increasing gasification and a combined fluidized bed 19a.
  • the mode of operation of the gasification reactor 4 is described in detail in the German patent application DE 10 2008 043 131.
  • the gasification reactor 4 makes it possible, through its special design and process management, almost completely to gasify a feedstock 16 with a high ash melting point (above 1 .000 ° C.), with pyrolysis in a fixed bed in a pyrolysis zone 24 and gasification in a reduction zone 19 at the same time the pyrolysis coke 8 takes place in a fluidized bed 19a.
  • a nearly tarry gas can be generated at almost complete conversion of the feedstock 16.
  • Due to the special process control the operating temperatures of the gasification reactor 4 are even in the hot oxidation zone 18 at only 850 ° C.
  • the structural design of the gasification reactor 4 is kept very simple.
  • the organic feedstock 3 having a low ash melting point in the pyrolysis reactor 2 is converted into pyrolysis gas 5 and pyrolysis coke 8 in a manner known per se.
  • the pyrolysis reactor 2 is presently designed as a pyrolysis tube and has a conveyor 9, in this case a screw conveyor, for the feedstock 3.
  • the screw conveyor is driven by means of a corresponding drive 10.
  • the conveyor 9 with the drive 10 offers the advantage that the feedstock 3 can be conveyed downwards at different speeds in accordance with the gasification rate of the pyrolysis reactor 2.
  • the pyrolysis reactor 2 also has a feed 25 for the organic feedstock 3 and at its opposite end a discharge opening 26 for pyrolysis coke 8.
  • an outlet 27 is arranged for the pyrolysis gas 5. If, as shown here, the outlet 27 for the pyrolysis gas 5 is arranged in an upper region of the pyrolysis reactor 2 and the discharge opening 14 in a lower region, separation of the solid and gaseous pyrolysis products can take place almost automatically by gravity.
  • the pyrolysis gas 5 produced in the pyrolysis reactor 2 is first of all deashed in a separation device 13 and finally fed to the gasification reactor 4.
  • the separation device 13 may be formed, for example, as a cyclone. This has at its lower end to a discharge opening 14 for ashes.
  • the ashless, tar-containing pyrolysis gas 5 is fed to the gasification reactor 4 below a carbon bed 7.
  • the gasification reactor 4 consists according to the present representation of a conically widening upwardly reaction space 15, which is fed against the gravitational force from below with a feedstock 16 with high ash melting point 16, such as wood.
  • the gasification reactor 4 has a feed 22 for the feedstock 16 and a gasification medium 17.
  • the gasification reactor 4 has a gas collection chamber 23 and an outlet 27 for the product gas 6.
  • a pyrolysis zone 24, an oxidation zone 18 and a reduction zone 19 are formed in layer form above the feedstock 16 in the reaction space.
  • the feedstock 16 hereby becomes substantially continuous conveyed upward and flowed through by the gasification medium 17 from below, so that the reduction zone 19 partially or completely forms with appropriate process control as a fluidized bed 19a.
  • the feedstock 16 with the high ash melting point is in this case almost completely converted to a low-tarry gas, so that the gasification reactor 4 generates a usable product gas 6 in addition to the pyrolysis gas 5 produced in the pyrolysis reactor 2.
  • the product gas 6 of the process according to the invention thus consists of the purified pyrolysis gas 5 and the gas additionally generated by the gasification reactor 4. Due to the almost complete conversion of the feedstock 16 and the generation of additional product gas 6 through the cracking unit or the gasification reactor 4, a very good overall efficiency of the plant 1 can be achieved.
  • the gasification reactor 4 further includes a feed 20 for water or steam.
  • the feed 20 is connected to an inlet 21 of the gasification reactor 4 for the pyrolysis gas 5, but this can also open separately into the gasification reactor 4.
  • the inlet 21 and the feed 20 can be designed, for example, in the form of an annular nozzle.
  • the energy for starting and optionally for maintaining the pyrolysis process in the pyrolysis reactor 2 is supplied by the hot product gas 6 from the gasification reactor 4.
  • the outlet 12 of the gasification reactor 4 is for this purpose connected to a heating jacket 1 1 of the pyrolysis reactor 2.
  • the substantially tar-free product gas 6 flows through the heating jacket 1 1 in countercurrent to the material flow of the feedstock 3 and is thereby cooled, so that no further cooling means for the product gas 6 are required.
  • By supplying the product gas 6 in countercurrent can a particularly good cooling of the product gas 6 and at the same time a faster heating of the organic feedstock 3 in the pyrolysis reactor 2 can be achieved.
  • the now cooled product gas 6 can be removed at the upper end of the heating mantle 1 1 or the pyrolysis reactor 2 and without further purification of its further utilization, for example a gas engine, are supplied.
  • the pyrolysis coke 8 can finally be discharged via the discharge opening 26 from the pyrolysis reactor 2 and fed to a further utilization.
  • the pyrolysis coke 8 can be used, for example, as a biofertilizer or, since it still represents an energy store, can be externally gasified or incinerated. It is particularly advantageous if the feedstock 3 in pelletized form is fed to the pyrolysis reactor 2, since the feedstock 3 largely retains its shape during pyrolysis and can thus be removed at the discharge opening 26 in a form which is capable of good transport and can be further utilized.
  • the present invention thus makes it possible to produce an almost tar-free product gas 6 by simultaneously reacting two feedstocks 3, 16 in two spatially separate reactors 2, 4 also from organic feedstocks 3 with a low ash melting point. Due to the spatial separation of the pyrolysis of the feedstock 3 with the low ash melting point and the further implementation of the pyrolysis gas 5 problems can be avoided by the low ash melting point, such as aggravated ash discharge and damage to equipment by slagging. By means of the system 1 according to the invention, it is thus possible to gasify virtually all of the organic starting materials, regardless of their ash melting point, virtually free of tar.
  • the gasification reactor 4 primarily serves to react the tars of the pyrolysis gas 5 and not the production of product gas 6 and is dimensioned with respect to the amount of the pyrolysis gas 5, the throughput of the feedstock 16 in comparison to the throughput of the feedstock 3 with low Ash melting point 3 are kept very low.
  • the overall efficiency of the system 1 or the process is high here, since the cracking unit designed as a gasification reactor itself generates part of the product gas and the heat from the cracking unit at the same time serves to maintain the pyrolysis process in the pyrolysis reactor 2, so that no external energy supply is required. At the same time no energy with the product gas 6 is discharged from the system 1. Due to the very cost-effective starting materials 16, the plant 1 according to the invention can thus be operated very economically and in contrast to a pure wood gasification subsidy independent. In principle, however, it is also conceivable to also use the gasification reactor 4 to produce a significant amount of product gas 6 and to design it correspondingly large.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention a pour objet une installation (1) pour la production d'un gaz de produit (6) à partir de matières premières organiques présentant un bas point de fusion des cendres (3), comprenant un réacteur de pyrolyse (2) pour le séchage et la pyrolyse de la matière première organique (3). Le réacteur de pyrolyse (2) comporte un orifice de sortie (27) pour un gaz de pyrolyse contenant du goudron (5) et une ouverture de décharge (26) pour un coke de pyrolyse carboné (8). L'installation comprend en outre une unité de craquage disposée en aval pour le craquage des goudrons contenus dans le gaz de pyrolyse (5) et conçue comme un réacteur de gazéification (4). Le réacteur de gazéification (4) comprend un orifice d'entrée (21) pour le gaz de pyrolyse (5) issu du réacteur de pyrolyse (2) et un orifice de sortie (12) pour le gaz de produit (6). Dans un procédé pour la production d'un gaz de produit (6) à partir de matières premières organiques (3) possédant un bas point de fusion des cendres, un gaz de pyrolyse contenant du goudron (5) et un coke de pyrolyse carboné (8) sont produits à partir de la matière première organique (3), et le gaz de pyrolyse (5) et le coke de pyrolyse (8) sont ensuite traités ultérieurement de façon séparée. Le gaz de pyrolyse contenant du goudron (5) est conduit dans un réacteur de gazéification (4) pour craquer les goudrons contenus dans le gaz. Dans le réacteur de gazéification (4), une seconde matière première organique (16) possédant un point de fusion des cendres élevé est gazéifiée de façon à obtenir un gaz pauvre en goudron, les goudrons contenus dans le gaz de pyrolyse (5) étant décomposés sur un lit de carbone (7) du réacteur de gazéification (4).
PCT/EP2010/067915 2009-12-03 2010-11-22 Installation pour la production d'un gaz de produit à partir de matières premières organiques WO2011067130A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102009047445A DE102009047445A1 (de) 2009-12-03 2009-12-03 Anlage zum Erzeugen eines Produktgases aus organischen Einsatzstoffen
DE102009047445.5 2009-12-03

Publications (1)

Publication Number Publication Date
WO2011067130A1 true WO2011067130A1 (fr) 2011-06-09

Family

ID=43598022

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2010/067915 WO2011067130A1 (fr) 2009-12-03 2010-11-22 Installation pour la production d'un gaz de produit à partir de matières premières organiques

Country Status (2)

Country Link
DE (1) DE102009047445A1 (fr)
WO (1) WO2011067130A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103254941A (zh) * 2013-05-29 2013-08-21 北京化工大学 一种高温循环加热流化床热解制气系统
CN103979491A (zh) * 2014-05-20 2014-08-13 青岛理工大学 一种污泥与生物质共混气化制氢的方法与装置
CN105290084A (zh) * 2015-11-07 2016-02-03 朱永彪 有机生物真空热解器
CN109963928A (zh) * 2016-10-07 2019-07-02 美瓦能源有限公司 改进的气化系统和方法

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012025478A1 (de) 2012-12-29 2014-07-03 Robert Völkl Verfahren und Vorrichtung zur Verwertung kohlenstoffhaltiger Asche
AT14489U1 (de) 2013-12-18 2015-12-15 Syncraft Engineering Gmbh Verfahren und Vorrichtung zum Austragen von Störstoffen
DE102014113307B4 (de) * 2014-09-16 2017-11-23 Gesellschaft Für Energie- Und Verfahrenstechnik Mbh Reaktor und Verfahren zur Erzeugung eines Brenngases aus mechanisch entwässertem Schlamm
IT202000025321A1 (it) 2020-10-26 2022-04-26 Ers Eng S R L Processo di gassificazione di materiale organico e impianto per attuare un tale processo
DE102021133899A1 (de) 2021-12-20 2023-06-22 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung eingetragener Verein Pyrolyseverfahren und Pyrolysevorrichtung zur Herstellung von Pyrolysegas und Pyrolysekoks
CN114479953B (zh) * 2022-01-27 2023-03-21 华中科技大学 一种利用生物质制备合成气的装置

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4030644A1 (de) * 1990-09-25 1992-03-26 Sanhog Technik Dr Ing Horst Ga Verfahren zur erzeugung brennbarer gase mit anschliessender gasumwandlung in einem bewegten koksbett
DE19945771C1 (de) 1999-09-24 2001-02-22 Muehlen Gmbh & Co Kg Dr Verfahren zur Vergasung von organischen Stoffen und Stoffgemischen
US6669822B1 (en) * 1998-10-28 2003-12-30 Ebara Corporation Method for carbonizing wastes
DE102008043131A1 (de) 2008-10-23 2010-04-29 Burkhardt Gmbh Verfahren und Vorrichtung zum thermochemischen Vergasen fester Brennstoffe

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2432504B2 (de) * 1974-07-04 1976-12-16 Kiener, Karl, Dipl.-Ing., 7080 Goldshöfe Verfahren und anlage zum herstellen von brenngasen aus stueckigem haus- und industriemuell u.dgl.
DE3144919A1 (de) * 1981-11-12 1983-05-19 Fritz Werner Industrie-Ausrüstungen GmbH, 6222 Geisenheim "verfahren zum aufbereiten von biomassen und einrichtung zur durchfuehrung des verfahrens"
DE10348142B3 (de) * 2003-10-10 2005-04-14 Circutec Focus On Future Gmbh Verfahren und Anlage zur Erzeugung von Synthesegas aus Reststoffen
DE102007036514A1 (de) * 2007-08-01 2009-02-05 Silber, Wolfgang Verfahren und Vorrichtung zur Erzeugung eines Synthesegases aus einem biogenen Stoff

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4030644A1 (de) * 1990-09-25 1992-03-26 Sanhog Technik Dr Ing Horst Ga Verfahren zur erzeugung brennbarer gase mit anschliessender gasumwandlung in einem bewegten koksbett
US6669822B1 (en) * 1998-10-28 2003-12-30 Ebara Corporation Method for carbonizing wastes
DE19945771C1 (de) 1999-09-24 2001-02-22 Muehlen Gmbh & Co Kg Dr Verfahren zur Vergasung von organischen Stoffen und Stoffgemischen
DE102008043131A1 (de) 2008-10-23 2010-04-29 Burkhardt Gmbh Verfahren und Vorrichtung zum thermochemischen Vergasen fester Brennstoffe

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
HAUK R ET AL: "VERGASUNGSVERFAHREN FUR ABFALLE", VGB KRAFTWERKSTECHNIK, VGB KRAFTWERKSTECHNIK GMBH. ESSEN, DE, vol. 74, no. 9, 1 September 1994 (1994-09-01), pages 790 - 796, XP000467877, ISSN: 0372-5715 *

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103254941A (zh) * 2013-05-29 2013-08-21 北京化工大学 一种高温循环加热流化床热解制气系统
CN103979491A (zh) * 2014-05-20 2014-08-13 青岛理工大学 一种污泥与生物质共混气化制氢的方法与装置
CN105290084A (zh) * 2015-11-07 2016-02-03 朱永彪 有机生物真空热解器
CN109963928A (zh) * 2016-10-07 2019-07-02 美瓦能源有限公司 改进的气化系统和方法
CN109963928B (zh) * 2016-10-07 2021-05-07 美瓦能源有限公司 改进的气化系统和方法

Also Published As

Publication number Publication date
DE102009047445A1 (de) 2011-06-09

Similar Documents

Publication Publication Date Title
WO2011067130A1 (fr) Installation pour la production d'un gaz de produit à partir de matières premières organiques
WO2010003968A2 (fr) Procédé et dispositif pour produire du gaz de synthèse à faible teneur en goudrons à partir de biomasse
CH615215A5 (fr)
DE102004024672B4 (de) Vorrichtung und Verfahren zur Erzeugung eines teerfreien Schwachgases durch Vergasung von Biomasse
DE102009052902A1 (de) Niedertemperaturpyrolyse von Biomasse in der Wirbelschicht für eine nachfolgende Flugstromvergasung
WO2015158732A1 (fr) Système et procédé de traitement thermo-catalytique d'une matière et huile de pyrolyse fabriqué au moyen de ceux-ci
DE102010018197A1 (de) Verfahren und Vorrichtung zur Vergasung von Biomasse
EP3309240A1 (fr) Procédé et dispositif de gazéification de biomasse
DE102008043131B4 (de) Verfahren und Vorrichtung zum thermochemischen Vergasen fester Brennstoffe
DE202014005809U1 (de) Vorrichtung zur Reinigung und Gewinnung von energiehaltigen Gasen
DE102006013617B4 (de) Biomassevergaser
EP3792216B1 (fr) Intégration thermique lors de la génération des gaz de synthèse par oxydation partielle
EP3214155B1 (fr) Procédé pour la production de gaz de synthèse pour la combustion dans un moteur à combustion interne.
EP2233551B1 (fr) Procédé et dispositif de gazage de matériaux organiques
DE112007003339T5 (de) Verfahren und Vorrichtung zur Vergasung von Vergasungsbrennstoff
WO2010149148A2 (fr) Procédé et dispositif de production de gaz pauvre et de charbon de bois à partir de combustibles solides
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
EP3088492B1 (fr) Procédé et dispositif de gazéification de biomasse
EP1399527B1 (fr) Procede et dispositif pour pyrolyser et gazeifier des melanges de matieres a composants organiques
AT520769A1 (de) Verfahren zum betreiben einer Anlage zur Energiegewinnung und Anlage hierfür
EP3067407B1 (fr) Système et méthode pour la gazéification de matière carbonée
DE10228100B4 (de) Verfahren und Vorrichtung zur Pyrolyse und Vergasung von Stoffgemischen, die organische Bestandteile enthalten
DE10312603B4 (de) Verfahren und Vorrichtung zur Vergasung und Verbrennung stückiger nachwachsender Rohstoffe in Form tierischer Knochen
AT516987B1 (de) Verfahren zum Kühlen eines heißen Synthesegases
EP2875102A1 (fr) Gazéification à contre-courant/co-courant de substances riches en carbone

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 10781503

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 10781503

Country of ref document: EP

Kind code of ref document: A1