EP0155930A2 - Procédé et installation pour la gazéification de matières carbonacées - Google Patents

Procédé et installation pour la gazéification de matières carbonacées Download PDF

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Publication number
EP0155930A2
EP0155930A2 EP85890063A EP85890063A EP0155930A2 EP 0155930 A2 EP0155930 A2 EP 0155930A2 EP 85890063 A EP85890063 A EP 85890063A EP 85890063 A EP85890063 A EP 85890063A EP 0155930 A2 EP0155930 A2 EP 0155930A2
Authority
EP
European Patent Office
Prior art keywords
gasified
heat
gasification
reactor
fiber
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.)
Withdrawn
Application number
EP85890063A
Other languages
German (de)
English (en)
Other versions
EP0155930A3 (fr
Inventor
Bruno Dr. Dipl.-Ing. Hillinger
Georg Dr. Dipl.-Ing. Beckmann
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.)
Waagner Biro AG
Original Assignee
Waagner Biro AG
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 Waagner Biro AG filed Critical Waagner Biro AG
Publication of EP0155930A2 publication Critical patent/EP0155930A2/fr
Publication of EP0155930A3 publication Critical patent/EP0155930A3/fr
Withdrawn legal-status Critical Current

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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
    • C10J3/06—Continuous processes
    • C10J3/12—Continuous processes using solid heat-carriers
    • 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
    • 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
    • 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
    • C10J2300/0983—Additives
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Definitions

  • the invention relates to a process for the gasification of carbon-containing fine-grained or sludge-like materials, such as e.g. Lignite dust or biomass in fixed bed reactors, in which the material to be gasified is preheated and, in particular, dried before entering the fixed bed reactor and the vapors formed are mixed with the gasification medium, coarse-grained fibers being added to the material to be gasified in or before the fixed bed reactor to improve the gas permeability .
  • carbon-containing fine-grained or sludge-like materials such as e.g. Lignite dust or biomass in fixed bed reactors
  • the material to be gasified must be introduced into the fixed bed reactor designed as a gasification reactor in a predetermined minimum grain size. If the grain size is less than this, there is a lack of gassing, as a result of which the efficiency of the system drops sharply. Furthermore, the substances to be gasified should have a Minoestas content so that after the gasification zone there is still a substance for gas distribution and also for gas heating. For the reasons mentioned, dusts, sawdust and sewage sludge can only be gasified to a very limited extent and can be recycled for thermal purposes. However, because of their changing low carbon content, washing piles that occur in coal mining are unsuitable for gasification and can practically only be deposited.
  • the object of the invention is to overcome these disadvantages even further and to provide the fixed bed reactor designed as a gasification reactor with a broader range of fuels by including the fine-grained or sludge-like materials.
  • the process according to the invention is characterized in that washing piles or limestone with a grain size of more than 10 mm are used as dietary fibers, which after separation from the ashes in the granular state are fed to a separate utilization and that ashes from the fixed bed reactor with the abrasion of the dietary fibers is applied to the moist material to be gasified and reacted, the Mg and Ca oxides contained in the ash being hydrated by the moisture of the materials introduced, and the material to be gasified being preheated and partially dried by the heat of reaction.
  • Essential embodiments of the invention are specified in the subclaims.
  • the invention is shown, for example and schematically, in the attached figure. That too gasifying material is fed via the feed line 1 via a mixing container 2 to a dryer 3, which is designed, for example, as a heated vibrating trough in which the material to be dried is dried and preheated by supplying heat. With the material to be gasified, the coarse-grained ballast material, such as preheated iron balls, limestone or washing piles, is also fed to the dryer via the line 4 and intimately mixed with the material to be gasified in the vibration channel of the dryer 3. Since the coarse grain load material has a higher temperature than the material to be gasified, additional heat is introduced, which results in a drying effect.
  • a dryer 3 which is designed, for example, as a heated vibrating trough in which the material to be dried is dried and preheated by supplying heat.
  • the coarse-grained ballast material such as preheated iron balls, limestone or washing piles
  • the vapors produced in the dryer are discharged via the steam line 5 and mixed with the gasification agent, which is fed via the feed line 6 to the gas distributor 7 in the actual gasification reactor.
  • the predried material is transferred from the dryer 3 into the solid-state reactor 8 according to arrow 9 and deposited there in layers, the temperature of the layers increasing from top to bottom to the actual gasification zone and after the gasification zone up to approximately the supply temperature of the gasification agent in the area of the gas distributor 7 drops again.
  • the degassed material now comes into a separation zone 10, in which a sieve 11 is provided, which separates the coarse-grained fiber from the ashes produced.
  • the ballast is fed to line 4, while the ash is discharged via the ash removal line 12 or recirculated via line 13, in particular if it contains a large amount of CaO or MgO, and is introduced into the mixing container 2, where the MgO or Ca0 reacts with the moisture of the material to be gasified, which causes the material to be dried to heat up in the mixing container, whereby the CaO or MgO is hydrated.
  • the hot generated in the fixed bed reactor 8 Fuel gas is discharged via line 14 and cooled in a heat exchanger 15, heat transfer being provided to the coarser-grained fiber, whereby part of the heat is used in the process for preheating the material to be gasified or for drying it.
  • Artificial fiber such as e.g. Iron body, ceramic or expanded clay body in spherical form or as zylpebbs.
  • natural fiber such as Wash mountains or limestone can be used.
  • washing mountains there is an additional introduction of material to be gasified in the form of carbon inclusions, whereby the material not to be gasified, insofar as it contains lime or magnesite, is also partially used.
  • limestone is used, the limestone can burn in the solid-fuel reactor 8 in this process, so that burnt lime is formed as coarse-grained fiber, which is fed to a separate recycling process, whereby the recirculation line shown in the drawing is interrupted and only the fresh lime via the heat exchanger 15 is supplied.
  • the gas permeability in the solid-state reactor can be improved, as a result of which a uniform temperature distribution is achieved in this reactor, which is expressed in better gasification efficiency.
  • the method according to the invention also enables the gasification of extremely low-ash fuels, which are obtained, for example, in biotechnology, as a result of which, for example, dewatered bagasse can be gasified.
  • the tar droplets which are discharged from the solid reactor 8 by the hot gas, partly in the heat exchanger 15 to the relatively cold dietary fibers are released, where they condense on their surface. This measure makes the fiber sticky, so that dust to be gasified sticks to the fiber.
  • the recirculated tar is then reintroduced into the solid-state reactor and can be converted into fuel gas or can be used directly as fuel by contacting the gasification medium, whereby the tar level in the circuit keeps itself at a certain level.
  • the dryer 3 is also possible to design the dryer 3 as a shaft dryer and to place it on the carburetor 8 after reducing the cross-section, which results in a retort in tower construction.
  • the line 14 for the hot fuel gas connects to the upper end of the retort, which in particular is still enlarged, as a result of which gas re-suction from the gasification chamber 8 into the dryer 3 and explosions in the dryer appear to be avoidable.
  • the dryer 3 thus forms a bulk material feed for the carburetor 8, from which, according to the volume reduction during gasification and the ash and fiber removal, dried or pre-dried bulk material flows.
  • a heat pipe system can also be provided, the heat absorption side of which is arranged in the wall of the gasifier 8 in the region of the gasification zone or just below it, and the heat emission side of which is arranged on the ceiling of the collecting chamber for the raw gas generated and rising from the gasification zone.
  • This part of the heat pipe system thus acts as a radiator and heats the respective free bulk material surface, which causes the gasification temperature of the Bulk goods and the ash discharge temperature is reached more quickly. This causes a reduction in the size of the gasifier or an increase in the specific gasification capacity of the gasifier.

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)
EP85890063A 1984-03-22 1985-03-15 Procédé et installation pour la gazéification de matières carbonacées Withdrawn EP0155930A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT962/84 1984-03-22
AT0096284A AT387786B (de) 1984-03-22 1984-03-22 Verfahren zur vergasung von kohlenstoffhaeltigen materialien

Publications (2)

Publication Number Publication Date
EP0155930A2 true EP0155930A2 (fr) 1985-09-25
EP0155930A3 EP0155930A3 (fr) 1986-08-13

Family

ID=3503820

Family Applications (1)

Application Number Title Priority Date Filing Date
EP85890063A Withdrawn EP0155930A3 (fr) 1984-03-22 1985-03-15 Procédé et installation pour la gazéification de matières carbonacées

Country Status (3)

Country Link
US (1) US4758248A (fr)
EP (1) EP0155930A3 (fr)
AT (1) AT387786B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010015316A3 (fr) * 2008-08-05 2010-11-25 Krones Ag Procédé et dispositif de production de gaz de synthèse à partir de biomasse
EP2333033A2 (fr) 2009-10-06 2011-06-15 Politechnika Lubelska Procédé pour la production d'un combustible à partir de boues d'épuration

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19961437C2 (de) * 1999-12-20 2002-04-18 Kopf Ag Verfahren und Anlage zur Gewinnung von brennbarem Gas aus Klärschlamm
US20060180459A1 (en) * 2005-02-16 2006-08-17 Carl Bielenberg Gasifier
DE102007062414B4 (de) * 2007-12-20 2009-12-24 Ecoloop Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
DE102011121508A1 (de) 2011-12-16 2013-06-20 Ecoloop Gmbh Gegenstromvergasung mit Synthesegas als Arbeitsmedium
DE102012014161A1 (de) 2012-07-18 2014-02-20 Ecoloop Gmbh Gegenstrom-/Gleichstrom-Vergasung von kohlenstoffreichen Substanzen

Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US538908A (en) * 1895-05-07 Emile gobbe
US189576A (en) * 1877-04-17 Improvement in processes and apparatus for manufacturing gas
DE168873C (fr) * 1903-07-03
US795874A (en) * 1905-01-17 1905-08-01 Charles Whitfield Apparatus for the manufacture of combustible gas from peat.
US906793A (en) * 1908-02-28 1908-12-15 Charles J Greenstreet Process of producing gas.
AT64423B (de) * 1912-05-23 1914-04-10 Arthur Graham Glasgow Verfahren und Vorrichtung zum Destillieren von bituminöser Kohle oder sonstigem kohlenstoffhaltigen Material.
US1977684A (en) * 1927-10-01 1934-10-23 Babcock & Wilcox Co Process of producing water gas
US2175613A (en) * 1936-03-10 1939-10-10 Koppers Co Inc Process for the production of gases
GB620029A (en) * 1945-01-16 1949-03-18 Edvin Andreas Johansson Improvements in methods for dry distillation
US2682455A (en) * 1949-06-16 1954-06-29 Consolidation Coal Co Gasification of carbonaceous solid fuels
US2591595A (en) * 1949-09-29 1952-04-01 Standard Oil Dev Co Method for controlling the temperature of exothermic reactions such as the gasification of carbonaceous solids
GB1435089A (en) * 1972-11-09 1976-05-12 Gen Electric Fixed bed coal gasification
DE2264924A1 (de) * 1972-11-17 1975-08-28 Gen Electric Verfahren zur erzeugung eines gasgemisches
US3920417A (en) * 1973-06-29 1975-11-18 Combustion Eng Method of gasifying carbonaceous material
DE2943309C2 (de) * 1979-10-26 1984-06-20 Hölter, Heinz, Dipl.-Ing., 4390 Gladbeck Verfahren zur gemeinsamen Pyrolyse von Ballastkohle und Müll mit anschließender Vergasung und Anlage zur Durchführung der Pyrolyse
DE3102819A1 (de) * 1980-01-29 1982-02-18 Babcock-Hitachi K.K., Tokyo Verfahren fuer die rueckgwinnung von waerme bei der kohlevergasung und vorrichtung dafuer
US4353713A (en) * 1980-07-28 1982-10-12 Cheng Shang I Integrated gasification process
DE3220126A1 (de) * 1982-05-28 1983-12-01 Eisenmann KG Maschinenbau-Gesellschaft mbH & Co, 7030 Böblingen Verfahren und anlage zur gewinnung von generatorgas aus fossilen brennstoffen

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010015316A3 (fr) * 2008-08-05 2010-11-25 Krones Ag Procédé et dispositif de production de gaz de synthèse à partir de biomasse
EP2333033A2 (fr) 2009-10-06 2011-06-15 Politechnika Lubelska Procédé pour la production d'un combustible à partir de boues d'épuration

Also Published As

Publication number Publication date
EP0155930A3 (fr) 1986-08-13
AT387786B (de) 1989-03-10
ATA96284A (de) 1988-08-15
US4758248A (en) 1988-07-19

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Inventor name: BECKMANN, GEORG, DR. DIPL.-ING.

Inventor name: HILLINGER, BRUNO, DR. DIPL.-ING.