EP1749872A2 - Méthode de gazéification endothermique de charbon - Google Patents

Méthode de gazéification endothermique de charbon Download PDF

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Publication number
EP1749872A2
EP1749872A2 EP20060013110 EP06013110A EP1749872A2 EP 1749872 A2 EP1749872 A2 EP 1749872A2 EP 20060013110 EP20060013110 EP 20060013110 EP 06013110 A EP06013110 A EP 06013110A EP 1749872 A2 EP1749872 A2 EP 1749872A2
Authority
EP
European Patent Office
Prior art keywords
gas
carbon
gasification
endothermic
endothermic gasification
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.)
Ceased
Application number
EP20060013110
Other languages
German (de)
English (en)
Other versions
EP1749872A3 (fr
Inventor
Dietmar Rüger
Olaf Schulze
Jonas Kappeller
Burkhard MÖLLER
Bodo Max Wolf
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.)
Linde GmbH
Original Assignee
Choren Industries 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 Choren Industries GmbH filed Critical Choren Industries GmbH
Publication of EP1749872A2 publication Critical patent/EP1749872A2/fr
Publication of EP1749872A3 publication Critical patent/EP1749872A3/fr
Ceased 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C10J3/487—Swirling or cyclonic gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/52—Ash-removing devices
    • C10J3/526—Ash-removing devices for entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—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
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1609—Post-reduction, e.g. on a red-white-hot coke or coal bed

Definitions

  • the invention relates to a process for the gasification of solid carbon with hot gases from the partial oxidation of gaseous, liquid and solid fuels, in particular coal, biomass and organic residues, e.g. from the treatment of waste, in the stream of air.
  • the field of application of the invention is the production of fuel, synthesis and reducing gas from these fuels.
  • the gasification of solid carbon with hot gases has been known since the introduction of the processes for the production of gas by partial oxidation in a fixed bed and in the fluidized bed.
  • the hot, carbon dioxide-containing gas is generated by burning solid carbon in the flow direction of the gasification before a so-called reduction zone.
  • the gas carries the gasifying agent carbon dioxide and the enthalpy required for the endothermic gasification of carbon to carbon monoxide into the reduction zone. Partial oxidation and endothermic gasification of carbon in the fixed-bed gasification thus occur sequentially, locally separated and at different temperatures.
  • the basic principle of this process is that solid carbon in the form of coal or coke, from the degassing of fuels, is mixed into a more than 1,200 ° C, partial stream of carbon dioxide and water vapor containing gas stream.
  • the carbon reacts with the gas components carbon dioxide and water vapor to form carbon monoxide and hydrogen, respectively, utilizing the physical enthalpy of the hot gas, i. part of the high-temperature physical enthalpy of the gas is converted back into chemical enthalpy by endothermic chemical reactions.
  • the calorific value of the gas increases, thereby improving the conversion efficiency of the process over those processes that only physically utilize the physical enthalpy of the gas.
  • the tar-containing degassing gas is in a combustion chamber according to the device DE 197 47 324 for the realization of the patent PCT / EP95 / 00443 together with the residual coke produced in the dedusting of the gasification gas above the ash melting point with an oxygen-containing gasification agent partially burned, so that a hot, tarry, in addition to CO and H 2 also CO 2 and H 2 O containing gasification agent is formed.
  • the fuel ash contained in the residual coke is melted.
  • the hot gasification agent flows out of the combustion chamber along with the liquid slag accordingly DE 197 47 324 in the form of a submersible jet in the arranged below the combustion chamber part of the entrained flow reactor in which run the endothermic reactions, hereinafter called endothermic entrained flow reactor.
  • the finely ground coke dust is injected pneumatically via lances and nozzles in the plunger jet and leads due to chemical quenching to a cooling of the gas and to increase the proportion of hydrogen and carbon monoxide.
  • the gas is deflected and leaves the apparatus together with the unreacted part of the coke, is then cooled by indirect heat removal and fed to the subsequent process stages.
  • the gas velocity in particular at the deflection point of the gas in the reactor and in the possibly upwardly flowing part must always be greater than the floating speed of the coke particles.
  • the relative velocity between coke and gas is low and the residence time of the coke is largely determined by the residence time of the gas, which in turn depends on the size of the endothermic reactor.
  • the endothermic gasification of solid carbon with water vapor and carbon dioxide is a process influenced by the reaction kinetics.
  • the rate of turnover of the solid carbon decreases with decreasing temperature and increasing proportions of carbon monoxide and hydrogen formed.
  • the gasification agent flows against the force of gravity from bottom to top.
  • the reactor cross section is dimensioned so that the gas velocity is below the levitation velocity of the fuel grain used.
  • the gas velocity is above the levitation velocity of the fuel grain.
  • the required fuel conversion is achieved by recycling the unreacted part of the fuel into the reaction zone of the reactor.
  • the aim of the invention is the further improvement of fuel utilization.
  • the technical problem is solved, in which the hot, down in the process flowing gas from the combustion chamber with separation of the liquid slag and the process stage endothermic gasification of solid carbon, which works with increasing gas flow, with the addition of solid carbon, preferably coke carbon an in-process carbonization and with a grain diameter of up to 20 mm, is supplied, wherein the Gas velocity at the carbon input above and at the end of the process stage endothermic gasification below the floating velocity of the reactive carbon particles.
  • the technical object of this example is the cooling of the hot gas from the combustion chamber, which was prepared by gasification of tar pyrolysis gas and residual coke from the raw gas dedusting with oxygen at a temperature of about 1400 ° C, by chemical quenching with the coking carbon from the same degassing from which the pyrolysis gas originates.
  • FIG. 1 represents a suitable device for carrying out the method according to the invention.
  • the tar-containing degassing gas 1, the residual coke dust 2 from the raw gas dedusting and the oxygen 3 are fed via separate channels of a swirl burner 4 of the combustion chamber 5.
  • the degassing gas and the residual coke react with the oxygen in the combustion chamber to form a gasification gas which, in addition to CO and H 2, also contains CO 2 and H 2 O and whose temperature is above the ash melting temperature of the residual coke ash. Due to the high temperature, the ash of the residual coke is melted and thrown by the swirl of the burner to the combustion chamber wall, on which the liquid slag runs off in the direction of the gas outlet from the combustion chamber 6.
  • a deflection chamber 7 is arranged below the combustion chamber, the side has a horizontal gas outlet 8 in the direction of a transition line 9.
  • a slag discharge opening 10 is arranged below it, filled with water slag bath 11th
  • the hot gas from the combustion chamber is deflected sharply in the deflection chamber in the direction of the transition line. Due to the centrifugal forces occurring, the fine slag droplets contained in the gas stream are separated from the gas stream and, together with the large slag particles dripping off the wall of the gas outlet 6, are thrown against the wall of the deflection chamber. From there, the liquid slag passes through the opening 10 in the slag bath 11 filled with water, where it solidifies to a solid granules, which is discontinuously discharged via the lock 12 from the reactor.
  • the deflected gas flows through the transition line 9 in a further deflection chamber 13, where it is deflected by 90 ° and passes through an opening 14 in the disposed over the chamber endothermic entrained flow reactor 15.
  • the coke 16 from the pyrolysis of the fuel with a coarse grain fraction to 20 mm is transported via a screw conveyor 17 in the endothermic entrained flow reactor.
  • the entrained flow reactor has an upwardly extending cross-section which is dimensioned such that the gas velocity at the lower end of the reactor is above the levitation velocity of the coarsest coke particles, so that no coke can fall in the direction of the diverting chamber 13 and the gas velocity at the upper end End below the levitation speed of the smallest, reactive coke particles is so leave the smallest, fully reacted particles with the gas stream the reactor.
  • the coarse coke particles are initially carried with the gas stream still up until the gas velocity decreases as a result of the widening reactor cross-section below the levitation speed, and then fall back until they are transported back up from the gas.
  • the design of the reactor and the selected grain structure of the coke causes an intensive mixing with large relative movements between coke and gas and an accumulation of coke in the reactor to a quasi-stationary state, which differs from the original coke gas Ratio after pyrolysis represents a coke surplus, ie with the invention it is possible to increase the ratio of solid carbon to gas from approximately 0.1 to greater than 1.
  • the raw gas laden with unreacted residual coke leaves the reactor through the gas outlet 18 and is cooled and dedusted before the actual use.
  • the residual coke 2 separated off in the dedusting passes back into the combustion chamber 5, as described above.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)
  • Processing Of Solid Wastes (AREA)
  • Hydrogen, Water And Hydrids (AREA)
EP20060013110 2005-07-28 2006-06-26 Méthode de gazéification endothermique de charbon Ceased EP1749872A3 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE102005035921A DE102005035921B4 (de) 2005-07-28 2005-07-28 Verfahren zur endothermen Vergasung von Kohlenstoff

Publications (2)

Publication Number Publication Date
EP1749872A2 true EP1749872A2 (fr) 2007-02-07
EP1749872A3 EP1749872A3 (fr) 2007-12-19

Family

ID=37311062

Family Applications (1)

Application Number Title Priority Date Filing Date
EP20060013110 Ceased EP1749872A3 (fr) 2005-07-28 2006-06-26 Méthode de gazéification endothermique de charbon

Country Status (7)

Country Link
US (1) US7776114B2 (fr)
EP (1) EP1749872A3 (fr)
CN (2) CN102212398B (fr)
AU (1) AU2006202676B2 (fr)
BR (1) BRPI0603010B1 (fr)
CA (1) CA2551313C (fr)
DE (1) DE102005035921B4 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008110383A2 (fr) * 2007-03-15 2008-09-18 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Gazéificateur
WO2009050494A2 (fr) * 2007-10-20 2009-04-23 Moulson Process Plant Limited Production de carburant à partir de déchets
WO2010099896A3 (fr) * 2009-03-04 2011-03-31 Uhde Gmbh Procédé et dispositif pour l'utilisation de l'enthalpie d'un gaz de synthèse par gazéification supplémentaire et postérieure de combustibles renouvelables
WO2011061299A1 (fr) 2009-11-20 2011-05-26 Rv Lizenz Ag Conversion thermochimique de matériaux carbonés, en particulier pour la production d'énergie sans émissions
WO2011032663A3 (fr) * 2009-09-18 2011-12-08 Uhde Gmbh Procédé de gazéification de résidu combinée de combustibles liquides et solides
WO2014183837A1 (fr) * 2013-05-16 2014-11-20 Linde Aktiengesellschaft Procédé et installation de gazéification au moins partielle d'un matériau d'alimentation organique solide

Families Citing this family (17)

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Publication number Priority date Publication date Assignee Title
DE102008032957A1 (de) 2008-07-12 2010-01-14 Dinano Ecotechnology Llc Verfahren zur Gewinnung von synthetischem Diesel
WO2012011800A1 (fr) * 2010-07-19 2012-01-26 Rl Finance B.V. Système et procédé de craquage thermique d'hydrocarbures comprenant une masse
US9115324B2 (en) 2011-02-10 2015-08-25 Expander Energy Inc. Enhancement of Fischer-Tropsch process for hydrocarbon fuel formulation
US9156691B2 (en) 2011-04-20 2015-10-13 Expander Energy Inc. Process for co-producing commercially valuable products from byproducts of heavy oil and bitumen upgrading process
US9169443B2 (en) 2011-04-20 2015-10-27 Expander Energy Inc. Process for heavy oil and bitumen upgrading
CN109135798B (zh) 2011-09-08 2021-04-06 强能公司 在gtl环境中用于制备烃类燃料的增强的费-托法
US9315452B2 (en) 2011-09-08 2016-04-19 Expander Energy Inc. Process for co-producing commercially valuable products from byproducts of fischer-tropsch process for hydrocarbon fuel formulation in a GTL environment
US8889746B2 (en) 2011-09-08 2014-11-18 Expander Energy Inc. Enhancement of Fischer-Tropsch process for hydrocarbon fuel formulation in a GTL environment
EP2584023A1 (fr) * 2011-10-21 2013-04-24 Neste Oil Oyj Procédé de production de composition de gaz de synthèse
EP2748284B1 (fr) * 2011-10-21 2021-07-21 Air Products And Chemicals, Inc. Procédé de gazéification
CA2776369C (fr) 2012-05-09 2014-01-21 Steve Kresnyak Amelioration du procede fischer-tropsch pour la formulation de combustibles hydrocarbones dans un environnement de conversion de gaz en liquide (gtl)
DE102013003413A1 (de) 2013-02-28 2014-09-11 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Abtrennung flüssiger Schlackepartikel
US9266730B2 (en) 2013-03-13 2016-02-23 Expander Energy Inc. Partial upgrading process for heavy oil and bitumen
CA2818322C (fr) 2013-05-24 2015-03-10 Expander Energy Inc. Procede de raffinage pour huile lourde et bitume
DE102014002842A1 (de) 2014-02-25 2015-08-27 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Flugstromvergasung von kohlenstoffreichem Material
EP3219777A1 (fr) 2015-12-09 2017-09-20 Ivan Bordonzotti Procede et installation pour la transformation de matériaux combustibles dans des gaz purifiés sans goudrons
CN114479950B (zh) * 2020-10-27 2023-07-28 中国石油化工股份有限公司 一种生物质热解气化制氢方法和系统

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DE19618213A1 (de) * 1996-05-07 1997-11-13 Petersen Hugo Verfahrenstech Verfahren zur Erzeugung von Brenngas und Anlage zur Durchführung des Verfahrens
WO2003033624A1 (fr) * 2001-10-16 2003-04-24 Forschungszentrum Karlsruhe Gmbh Procede de pyrolyse et de gazeification de biomasse

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DE19747324C2 (de) 1997-10-28 1999-11-04 Bodo Wolf Vorrichtung zur Erzeugung von Brenn-, Synthese- und Reduktionsgas aus nachwachsenden und fossilen Brennstoffen, Biomassen, Müll oder Schlämmen
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US3951615A (en) * 1973-05-18 1976-04-20 Dr. C. Otto & Comp. G.M.B.H. Cylindrical pressure reactor for producing a combustible gas
DE19618213A1 (de) * 1996-05-07 1997-11-13 Petersen Hugo Verfahrenstech Verfahren zur Erzeugung von Brenngas und Anlage zur Durchführung des Verfahrens
WO2003033624A1 (fr) * 2001-10-16 2003-04-24 Forschungszentrum Karlsruhe Gmbh Procede de pyrolyse et de gazeification de biomasse

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Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008110383A2 (fr) * 2007-03-15 2008-09-18 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Gazéificateur
WO2008110383A3 (fr) * 2007-03-15 2009-07-02 Mci Man Ct Innsbruck Internati Gazéificateur
WO2009050494A2 (fr) * 2007-10-20 2009-04-23 Moulson Process Plant Limited Production de carburant à partir de déchets
WO2009050494A3 (fr) * 2007-10-20 2009-09-11 Moulson Process Plant Limited Production de carburant à partir de déchets
KR101633951B1 (ko) 2009-03-04 2016-06-27 티센크루프 인더스트리얼 솔루션스 아게 재생연료를 추가 및 후-가스화하여 합성가스의 엔탈피를 이용하기 위한 방법 및 장치
KR20110139243A (ko) * 2009-03-04 2011-12-28 티센크루프 우데 게엠베하 재생연료를 추가 및 후-가스화하여 합성가스의 엔탈피를 이용하기 위한 방법 및 장치
US9234148B2 (en) 2009-03-04 2016-01-12 Thyssenkrupp Industrial Solution Ag Process and apparatus for the utilization of the enthalpy of a syngas by additional and post-gasification of renewable fuels
WO2010099896A3 (fr) * 2009-03-04 2011-03-31 Uhde Gmbh Procédé et dispositif pour l'utilisation de l'enthalpie d'un gaz de synthèse par gazéification supplémentaire et postérieure de combustibles renouvelables
WO2011032663A3 (fr) * 2009-09-18 2011-12-08 Uhde Gmbh Procédé de gazéification de résidu combinée de combustibles liquides et solides
CN102549117A (zh) * 2009-09-18 2012-07-04 蒂森克虏伯伍德公司 用于液体燃料和固体燃料的混合残渣气化的方法
RU2553156C2 (ru) * 2009-09-18 2015-06-10 ТюссенКрупп Уде ГмбХ Способ объединенной газификации остатков жидкого и твердого топлива
WO2011061299A1 (fr) 2009-11-20 2011-05-26 Rv Lizenz Ag Conversion thermochimique de matériaux carbonés, en particulier pour la production d'énergie sans émissions
US10450520B2 (en) 2009-11-20 2019-10-22 Rv Lizenz Ag Thermal and chemical utilization of carbonaceous materials, in particular for emission-free generation of energy
EP3594313A1 (fr) 2009-11-20 2020-01-15 RV Lizenz AG Conversion thermochimique de matériaux carbonés, en particulier pour la production d'énergie sans émissions
US10844302B2 (en) 2009-11-20 2020-11-24 Rv Lizenz Ag Thermal and chemical utilization of carbonaceous materials, in particular for emission-free generation of energy
WO2014183837A1 (fr) * 2013-05-16 2014-11-20 Linde Aktiengesellschaft Procédé et installation de gazéification au moins partielle d'un matériau d'alimentation organique solide

Also Published As

Publication number Publication date
EP1749872A3 (fr) 2007-12-19
CN1903997B (zh) 2011-07-27
CN1903997A (zh) 2007-01-31
US20070163176A1 (en) 2007-07-19
BRPI0603010A (pt) 2007-05-15
US7776114B2 (en) 2010-08-17
AU2006202676A1 (en) 2007-02-15
CN102212398B (zh) 2013-01-23
CN102212398A (zh) 2011-10-12
CA2551313C (fr) 2013-02-19
DE102005035921B4 (de) 2008-07-10
DE102005035921A1 (de) 2007-02-08
CA2551313A1 (fr) 2007-01-28
BRPI0603010B1 (pt) 2016-06-14
AU2006202676B2 (en) 2011-03-31

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