EP0948583B1 - Procede de gazeification de combustibles solides dans un lit fluidise en circulation - Google Patents

Procede de gazeification de combustibles solides dans un lit fluidise en circulation Download PDF

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Publication number
EP0948583B1
EP0948583B1 EP97952838A EP97952838A EP0948583B1 EP 0948583 B1 EP0948583 B1 EP 0948583B1 EP 97952838 A EP97952838 A EP 97952838A EP 97952838 A EP97952838 A EP 97952838A EP 0948583 B1 EP0948583 B1 EP 0948583B1
Authority
EP
European Patent Office
Prior art keywords
gas
solids
hydrocarbons
dust
separator
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.)
Expired - Lifetime
Application number
EP97952838A
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German (de)
English (en)
Other versions
EP0948583A1 (fr
Inventor
Johannes Albrecht
Johannes Loeffler
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.)
MG Technologies AG
Original Assignee
Metallgesellschaft AG
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Filing date
Publication date
Application filed by Metallgesellschaft AG filed Critical Metallgesellschaft AG
Publication of EP0948583A1 publication Critical patent/EP0948583A1/fr
Application granted granted Critical
Publication of EP0948583B1 publication Critical patent/EP0948583B1/fr
Anticipated expiration legal-status Critical
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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
    • C10J3/58—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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/58—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
    • 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
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas

Definitions

  • the invention relates to a process for gasifying solid fuels in the circulating fluidized bed, the fuels being gasified in a gasification reactor with the supply of oxygen-containing gas at temperatures in the range from 700 to 1000.degree. C., a gas-solid mixture from the upper area of the gasification reactor Separator feeds, from the separator dust and hydrocarbons including higher hydrocarbons with more than 6 carbon atoms in the molecule (C 6+ hydrocarbons) containing gas with a calorific value of 2000 to 8000 kJ / m 3 and separately separated solids and the solids leads at least partially back into the lower region of the gasification reactor.
  • the invention has for its object to modify the known methods so that the dust is removed dry and wet washing with the formation of waste water in the gas cleaning is eliminated. According to the invention, this is achieved in the process mentioned at the outset by passing the dust-containing gas from the separator through a cracking chamber, with the gas contained in the cracking chamber with the addition of gaseous oxygen in the temperature range from 800 to 1200 ° C.
  • Hydrocarbons largely splits and the content of the higher hydrocarbons (C 6+ hydrocarbons) in the gas is reduced to a maximum of 10% by weight of the content of these higher hydrocarbons in the gas coming from the separator by cooling the gas coming from the splitting chamber which conducts the cooled gas through a dedusting device and separates flue dust, that the cooled and dedusted gas is passed through at least one bed or a reactor with granular solids which binds pollutants and then dedusts the gas, and that at least part of the flue dust extracted from the dedusting device is removed s in a combustion chamber at temperatures in the range of 1000 to 1500 ° C with the addition of gas containing O 2 .
  • the solid fuels to be gasified can e.g. B. um municipal or industrial waste, biomass or coal act in different ways.
  • Municipal waste is gasified this is usually done before gasification pre-sorted, especially metal and glass parts be discarded.
  • the remaining waste is then still crushed, e.g. B. to piece sizes of at most 70 mm before it is gassed.
  • To increase the calorific value of the from the Gasification reactor coming gas can be the solid fuel dry before gasification.
  • the one from the bottom of the gasification reactor drawn ash is usually so inert that it z. B. still is usable for road construction, but at least the ashes are easy to deposit.
  • the one in the dust collector Air dust can be heavy metal and then disposed of in the usual way. You burn or gasifies at least part of the airborne dust in a combustion chamber at temperatures in the range of 1000 to 1500 ° C. It is recommended that in the combustion chamber formed gaseous products in the gasification reactor give.
  • the solid fuels to be gasified are fed in line (1) to a gasification reactor (2), where they come into contact with hot gases and particles in the state of the circulating fluidized bed.
  • Oxygen-containing fluidizing gas is introduced in line (3) and passed through a distribution chamber (4) with a grate (5) into the fluidized bed of the reactor (2).
  • the oxygen-containing gas in line (3) can be, for example, air or air enriched with O 2 .
  • the gasification in the reactor (2) takes place at temperatures of 700 to 1000 ° C and mostly at temperatures of at least 800 ° C.
  • Ash is drawn off through line (6) and, if necessary, is deposited after removal of metal components or for further use, e.g. B. in road construction.
  • the dust-containing gas of line (10) contains condensable hydrocarbons and mostly carbon-containing fly dusts. It is important to at least largely eliminate the higher hydrocarbons (C 6+ ) and convert them into substances that do not condense at the given temperatures and partial pressures.
  • the gas is passed through a cracking chamber (12) through which line (13) O 2 -containing gas, for. B. air, oxygen-enriched air or technically pure oxygen. Temperatures in the range from 800 to 1200 ° C and mostly 900 to 1100 ° C are ensured in the gap chamber (12). It is important here that the temperature and the residence time in the cracking chamber (12) are chosen so that the formation of liquid slag is avoided and at the same time an adequate cracking of the C 6+ hydrocarbons is ensured.
  • the gas coming from the gap chamber (12) in line (15) contains various types of solids and ash particles, which are here be referred to as flying dust.
  • a waste heat boiler (16) cooling the gas to temperatures of about 150 to 300 ° C and then there is one through line (17) Dedusting device (18).
  • This can be, for. B. um act a tissue or electrostatic precipitator.
  • the accruing Airborne dust which usually contains heavy metals, is in the Line (19) withdrawn, part of it can be transported (20) to a combustion chamber (21). The rest Airborne dust is removed from the process through line (22) away.
  • oxygen-containing gas for. B. air, enriched with O 2 or technically pure oxygen and burns the supplied dust at temperatures in the range of 1000 to 1500 ° C.
  • the resulting solid or liquid and gaseous combustion products are put together in the upper area of the reactor (2), where they are taken up by the fluidized bed. 1, liquid slag can also be drawn off from the combustion chamber (21) in such a way that it does not get into the reactor (2), see FIG. 2.
  • a gas which still contains an interfering content Has pollutants.
  • pollutants are e.g. B. mercury, chlorine and sulfur compounds.
  • the cooled gas is led through the Line (27) for cleaning, whereby the formation of Avoids waste water.
  • the gas to be cleaned is in contact with granular adsorbents brought.
  • These adsorbents can e.g. B. in a fixed bed, Moving bed or fluidized bed can be arranged or you can get one Use entrained flow reactor.
  • Moving bed reactor (30) shown which one through the line (31) feeds granular adsorbent material in the reactor (30) forms a bed (33) which slowly moves downwards.
  • the fill is approximately in the horizontal direction from to flows through cleaning gas.
  • the gas leaves the reactor (30) through the line (35) and is dusted by the filter (36) performed, for. B. a tissue or Can act electrostatic precipitator.
  • Cleaned gas leaves the filter (36) in line (37). That coming from the reactor (30) loaded adsorbent is removed in line (38), with the solids in the line separated in the filter (36) (39) mixed and subtracted.
  • Adsorption materials are particularly the following Options: hydrated lime, activated carbon, stove coke or Zeolites.
  • the mercury removal using a Low-aluminum zeolites are described in EP patent 638 351.
  • FIG. 2 gives the pollutant gas line (27) one Spray absorber (40), to which one passes through the line (41) milk of lime and possibly other adsorbents.
  • Gas and Solids flow through line (42) to a filter (43), which is e.g. B. can be a fabric or electrostatic filter can.
  • Chloride-containing solids are drawn off in line (45).
  • In the combustion chamber (21) is pulled through the liquid slag Line (23) and leads the combustion gas through the line (32) into the reactor (2).
  • Residual municipal waste is fed to a process according to FIG. 2.
  • the following data are partially calculated.
  • the residual waste which is delivered in an amount of 7500 kg / h, contains 24.5% by weight moisture and 30% by weight ash.
  • This waste is first dried to 5% by weight of residual moisture and then gasified in the reactor (2) at 900 ° C. and with the supply of 6230 Nm 3 / h of air.
  • the residence time of the gas in the gap chamber (12) is 1.5 seconds, air is supplied through line (13) and an outlet temperature of 1000 ° C. is reached.
  • the content of C 6+ hydrocarbons in line (15) is only 0.1% by volume.
  • 400 kg / h of dust are fed through the line (20) into the combustion chamber (21), which is fed with 1860 Nm 3 / h of air and in which 1300 ° C. can be reached.
  • Lime milk is added to the spray absorber (40) and the outlet temperature is kept at 160 ° C.
  • the adsorber (46) contains a zeolite fixed bed for mercury removal.

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

Claims (2)

  1. Procédé de gazéification de combustibles solides dans le lit fluidisé circulant, les combustibles étant gazéifiés dans un réacteur de gazéification (2) sous apport de gaz oxygéné à des températures du domaine de 700 à 1000°C, un séparateur (9) étant alimenté avec un mélange gaz-solides depuis la zone supérieure du réacteur de gazéification, du gaz chargé de poussières et d'hydrocarbures y compris d'hydrocarbures supérieurs contenant plus de 6 atomes C dans la molécule, d'une valeur calorifique de 2000 à 8000 kJ/m3, et, séparément, des solides séparés étant évacués hors du séparateur, et les solides étant ramenés au moins partiellement dans la zone inférieure du réacteur de gazéification, caractérisé en ce que le gaz chargé de poussières passe hors du séparateur (9) à travers une chambre de séparation (12), les hydrocarbures contenus dans le gaz étant largement décomposés dans la chambre de séparation sous apport d'oxygène gazeux à une température du domaine de 800 à 1200°C et en dessous de la température du point de fusion des cendres, et la teneur en hydrocarbures supérieures (hydrocarbures C6+) dans le gaz étant réduite à au plus 10 % de la teneur en poids de ces hydrocarbures supérieurs dans le gaz provenant du séparateur, en ce que le gaz provenant de la chambre de séparation est refroidi, le gaz refroidi passe à travers un dispositif de dépoussiérage (18), et les poussières volantes sont séparées, en ce que le gaz refroidi et dépoussiéré passe à travers au moins un lit ou un réacteur (40) avec des solides granuleux liant les substances nocives et le gaz est ensuite dépoussiéré, et en ce qu'on fait réagir au moins une partie des poussières volantes extraites du dispositif de dépoussiérage (18) dans une chambre de combustion (21) à des températures du domaine de 1000 à 1500°C sous addition de gaz oxygéné.
  2. Procédé selon la revendication 1, caractérisé en ce que les produits gazeux formés dans la chambre de combustion (21) sont mélangés au gaz contenant des solides formés dans le réacteur de gazéification (2).
EP97952838A 1996-12-18 1997-12-01 Procede de gazeification de combustibles solides dans un lit fluidise en circulation Expired - Lifetime EP0948583B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19652770A DE19652770A1 (de) 1996-12-18 1996-12-18 Verfahren zum Vergasen fester Brennstoffe in der zirkulierenden Wirbelschicht
DE19652770 1996-12-18
PCT/EP1997/006716 WO1998027182A1 (fr) 1996-12-18 1997-12-01 Procede de gazeification de combustibles solides dans un lit fluidise en circulation

Publications (2)

Publication Number Publication Date
EP0948583A1 EP0948583A1 (fr) 1999-10-13
EP0948583B1 true EP0948583B1 (fr) 2001-01-24

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EP97952838A Expired - Lifetime EP0948583B1 (fr) 1996-12-18 1997-12-01 Procede de gazeification de combustibles solides dans un lit fluidise en circulation

Country Status (8)

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EP (1) EP0948583B1 (fr)
JP (1) JP2001506288A (fr)
AU (1) AU722068B2 (fr)
BR (1) BR9714421A (fr)
CA (1) CA2275646A1 (fr)
DE (2) DE19652770A1 (fr)
ES (1) ES2155270T3 (fr)
WO (1) WO1998027182A1 (fr)

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JP2003326241A (ja) * 2002-05-14 2003-11-18 Mitsubishi Heavy Ind Ltd バイオマスのガス化装置
FI20055237L (fi) 2005-05-18 2006-11-19 Foster Wheeler Energia Oy Menetelmä ja laitteisto hiilipitoisen materiaalin kaasuttamiseksi
JP2009536260A (ja) 2006-05-05 2009-10-08 プラスコエナジー アイピー ホールディングス、エス．エル．、ビルバオ シャフハウゼン ブランチ 炭素質原料のガスへの変換のための制御システム
NZ573217A (en) 2006-05-05 2011-11-25 Plascoenergy Ip Holdings S L Bilbao Schaffhausen Branch A facility for conversion of carbonaceous feedstock into a reformulated syngas containing CO and H2
KR20090019816A (ko) 2006-05-05 2009-02-25 플라스코에너지 아이피 홀딩스, 에스.엘., 빌바오, 샤프하우젠 브랜치 가스 조절 시스템
BRPI0712491A2 (pt) 2006-05-05 2012-10-09 Plascoenergy Ip Holdings S L Bilbao sistema de homogeneização de gás para regular caracterìsticas de gás e processo para converter um gás de entrada a um gás regulado
US8435315B2 (en) 2006-05-05 2013-05-07 Plasco Energy Group Inc. Horizontally-oriented gasifier with lateral transfer system
US8475551B2 (en) 2006-05-05 2013-07-02 Plasco Energy Group Inc. Gas reformulating system using plasma torch heat
BRPI0822209A2 (pt) 2007-02-27 2019-09-24 Plascoenergy Ip Holdings S L Bilbao Schaffhausen Branch sistema de gaseificação com conversão de matéria-prima processada/carvão e reformulação de gás
EP2034003A1 (fr) * 2007-09-07 2009-03-11 ReSeTec Patents Geneva S.A. i.o. Procédé et appareil de production de gaz de synthèse à partir des déchets
DE102008035604A1 (de) * 2008-07-31 2010-02-04 Uhde Gmbh Vorrichtung und Verfahren zur Entgasung von Stäuben
DE102010006192A1 (de) * 2010-01-29 2011-08-04 Uhde GmbH, 44141 Verfahren zur Biomasse-Vergasung in einer Wirbelschicht
US9321640B2 (en) 2010-10-29 2016-04-26 Plasco Energy Group Inc. Gasification system with processed feedstock/char conversion and gas reformulation
SA113340700B1 (ar) * 2012-07-09 2015-10-13 ساوثرن كمبني تغويز أنواع فحم بيتيوميني كثير الرماد، وعند درجة حرارة صهر رماد عالية
CN103224813B (zh) * 2013-04-15 2014-11-05 中国五环工程有限公司 煤炭气化的加压流化床工艺及加压流化床系统
AT516987B1 (de) * 2015-03-24 2017-07-15 Gussing Renewable Energy Int Holding Gmbh Verfahren zum Kühlen eines heißen Synthesegases
DE102015015594A1 (de) 2015-12-04 2017-06-08 Wincip Gmbh Verfahren und Anlage zur Synthesegaserzeugung durch Vergasung von flüssigen, festen oder pastösen Kohlenstoffträgern in einer Wirbelschicht,
DE102018002086A1 (de) * 2018-03-09 2019-09-12 Borsig Gmbh Quenchsystem
CN110564453A (zh) * 2019-09-17 2019-12-13 昆明理工大学 一种分布式生物质气化与燃烧耦合的多联产系统和方法
CN112961695A (zh) * 2020-12-31 2021-06-15 童铨 一种固体废弃物绝氧热解及高温熔融处理工艺及系统
CN113263040B (zh) * 2021-03-26 2023-01-10 童铨 一种固体废弃物的低碳协同处理工艺

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DE4235412A1 (de) * 1992-10-21 1994-04-28 Metallgesellschaft Ag Verfahren zum Vergasen von brennbare Bestandteile enthaltenden Abfallstoffen
DE4412004A1 (de) * 1994-04-07 1995-10-12 Metallgesellschaft Ag Verfahren zum Vergasen von Abfallstoffen in der zirkulierenden Wirbelschicht

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DE4235412A1 (de) * 1992-10-21 1994-04-28 Metallgesellschaft Ag Verfahren zum Vergasen von brennbare Bestandteile enthaltenden Abfallstoffen
DE4412004A1 (de) * 1994-04-07 1995-10-12 Metallgesellschaft Ag Verfahren zum Vergasen von Abfallstoffen in der zirkulierenden Wirbelschicht

Also Published As

Publication number Publication date
CA2275646A1 (fr) 1998-06-25
EP0948583A1 (fr) 1999-10-13
DE59702967D1 (de) 2001-03-01
JP2001506288A (ja) 2001-05-15
WO1998027182A1 (fr) 1998-06-25
AU5657598A (en) 1998-07-15
DE19652770A1 (de) 1998-06-25
AU722068B2 (en) 2000-07-20
ES2155270T3 (es) 2001-05-01
BR9714421A (pt) 2000-05-02

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