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EP0030323A1 - Procédé de fonctionnement d'un réacteur à lit fluidisé pour gazéifier des matières carbonacées - Google Patents

Procédé de fonctionnement d'un réacteur à lit fluidisé pour gazéifier des matières carbonacées Download PDF

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Publication number
EP0030323A1
EP0030323A1 EP80107380A EP80107380A EP0030323A1 EP 0030323 A1 EP0030323 A1 EP 0030323A1 EP 80107380 A EP80107380 A EP 80107380A EP 80107380 A EP80107380 A EP 80107380A EP 0030323 A1 EP0030323 A1 EP 0030323A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
post
reaction space
temperature
reactor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP80107380A
Other languages
German (de)
English (en)
Other versions
EP0030323B1 (fr
Inventor
Friedrich H. Dr. Ing. Franke
Ernst Dipl.-Ing. Pattas
Wolfgang Dr. Adlhoch
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.)
Rheinbraun AG
Original Assignee
Rheinische Braunkohlenwerke 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
Priority claimed from DE19792949533 external-priority patent/DE2949533A1/de
Priority claimed from DE19803033115 external-priority patent/DE3033115A1/de
Application filed by Rheinische Braunkohlenwerke AG filed Critical Rheinische Braunkohlenwerke AG
Publication of EP0030323A1 publication Critical patent/EP0030323A1/fr
Application granted granted Critical
Publication of EP0030323B1 publication Critical patent/EP0030323B1/fr
Expired 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
    • C10J3/54—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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/503—Fuel charging devices for gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • 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
    • C10J2300/093—Coal
    • 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
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/0969—Carbon dioxide
    • 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
    • C10J2300/0976—Water as steam
    • 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 method for operating a fluidized bed reactor for the gasification of carbon-containing material using exothermic and endothermic gasifying agents with a post-reaction space located above the fluidized bed, through which the gas mixture emerging from the fluidized bed and carbon-containing solid particles flows, whereby gasifying agent into Fluidized bed and introduced into the post-reaction space via at least three injection areas arranged along the longitudinal axis of the reactor.
  • air, oxygen and hydrogen are suitable as exothermic gasifying agents and water vapor and CO 2 as endothermic gasifying agents.
  • gasifying carbonaceous material e.g. B. coal
  • carbon-containing solid particles having a fluidized bed and a post-reaction room above, in which entrained, carbon-containing solid particles are gasifying agent - z. B. oxygen and water vapor - to be blown
  • the gasifying agents blown into the lower region of the reactor also simultaneously effecting the fluidization of the fluidized bed.
  • additional gasifying agents above the upper limit of the fluidized bed. There is intended to ensure that the solid discharged upward from the fluidized bed is gasified as completely as possible on the way through the after-reaction space.
  • the temperature drops more or less continuously from a maximum just above the upper boundary of the fluidized bed to a much lower temperature in the upper region of the reaction space.
  • the temperature profile ie the temperature profile along the longitudinal axis in the after-reaction space, is of great importance for the operation of the reactor and also for the quality of the gas produced therein.
  • the temperature profile is also important for the greatest possible conversion of the carbon-containing material introduced into the reactor.
  • a high temperature in the presence of carbonaceous material favors the CO and H 2 T yield. If the ash melts, however, a temperature that is too high can lead to the caking already mentioned and to the formation of agglomerates which impair the operation of the reactor or even lead to interruptions in operation. Too low a temperature avoids difficulties due to melting the ash, but on the other hand leads to a higher C0 2 and H 2 0 content in the product gas.
  • the implementation of the solid carbon is also involved Co 2 and H 2 0 to CO and H 2 are not particularly favorable conditions.
  • the invention is based inter alia on the object of modifying the method of the type described in the introduction in such a way that, in view of the limits set by the ash melting point, the most complete possible implementation of the carbon-containing material located in the post-reaction space is effected.
  • the gasification agents introduced into the reactor should be selectively usable, so that the greatest possible effect in terms of extensive gasification of the solid carbon particles with the formation of usable gases can be achieved with the least possible expenditure on gasification agents.
  • the invention proposes to achieve this object proposes that the gasification agents be introduced into the post-reaction space so distributed along the longitudinal axis of the reactor that a temperature level which is as constant as possible along the reactor axis is maintained above the fluidized bed.
  • the gasification agents are introduced into the post-reaction space distributed along the longitudinal axis of the reactor in such a way that above the fluidized bed there are at least two distinct sections of the post-reaction space which extend over at least two blowing-in areas and in which the temperature levels are as constant as possible of different heights along the reactor axis. It also applies to the second section that the temperature is as constant as possible in the sense described above, it being optimally adjusted to match the carbon present or to be converted in this area.
  • Both of the above-mentioned possibilities of metering the gasification agents are based on the consideration that it is not only important to add as much gasification agent at one or possibly at two points that it is sufficient to convert the carbon present in the after-reaction space. This would correspond to e.g. B. that known mode of operation, in which only a comparatively large amount of gasifying agent is added only once, namely just above the fluidized bed, in order to achieve the greatest possible conversion of the carbon-containing solid particles discharged upward from the fluidized bed, the ratios being in the range above of the post-reaction space are more or less left to their own devices.
  • the implementation of the method according to the invention achieves a reaction in the entire post-reaction space which is directed over the longitudinal extent of the post-reaction space and leads to clear operating conditions, so that it is easier from the outset to optimally target the desired operating parameters, for example the temperature profile and, depending on this, the addition of gasifying agents to control.
  • the desired operating parameters for example the temperature profile and, depending on this, the addition of gasifying agents to control.
  • overheating which can lead to caking and thus to malfunctions, can be avoided in this way despite a high mean temperature.
  • the gasification agents can be supplied in the usual manner.
  • the distances between the individual blowing areas or levels can be constant.
  • the gas and solid mixture emerging from the top of the fluidized bed essentially has the temperature which is to be maintained in the after-reaction space or in the lower section thereof.
  • a correspondingly stronger addition of exothermic gasifying agent just above the fluidized bed can initially bring about a temperature increase to the temperature level to be maintained in the after-reaction space.
  • the addition of the gasification agents in the individual blowing areas can be controlled depending on the temperature determined there. It is also possible to add the gasifier depending on others To control parameters, for example of the carbon content of the solid particles of the gas-solid mixture flowing through the after-reaction space.
  • the gasifier depending on others
  • To control parameters for example of the carbon content of the solid particles of the gas-solid mixture flowing through the after-reaction space.
  • a feed device indicated at 12 which can be designed as a screw or otherwise in a suitable manner.
  • a fluidized bed 15 is built up, the upper and lower limits of which are designated 16 and 17, respectively.
  • a layer 18 Below the lower boundary 17 there is a layer 18, the at least predominantly containing ash. Parts are discharged through an opening 19 located at the lower end of the reactor 10.
  • the gasification agents which cause the swirling of the bed 15 can normally be oxygen-containing gasification agents, that is to say an exothermic reaction, and steam and / or CO 2 , that is to say an endothermic reaction gasification agents.
  • the gases can arrive via nozzles, several of which are distributed over the circumference of the reactor. are ordered, are blown in, it is possible to effect endothermic gasifying agents and exothermic gasifying agents in two separate, e.g. B. feed superimposed areas or levels.
  • the post-reaction space 20 located above it by the gas mixture flowing upwards.
  • the latter is firstly the gaseous reaction products from the fluidized bed and secondly residues of the unreacted gasifying agents, in particular steam.
  • the solid particles still contain carbon, which is to be reacted within the post-reaction space.
  • the heat required for this is supplied by burning part of the combustible gases contained in the gas mixture, essentially CO and H 2 , and part of the carbon-containing solid.
  • the necessary means e.g. B.
  • oxygen is injected through lines and nozzles, which are distributed along the longitudinal axis of the reactor above the fluidized bed 15 in the post-reaction space 20th and are designated 21, 23, 25 and 27. It also applies here that a plurality of lines or nozzles can open into the post-reaction space and flow into it. Furthermore, gasification agent is blown into the after-reaction space 20 through the nozzles 21, 23, 25, and 27. It is possible to inject exothermic gases on the one hand and endothermic gases on the other hand as a mixture or through separate supply systems and nozzles. In the temperature profile shown in FIG. 1 in addition to the reactor 10, the levels in which gasification agents are introduced into the after-reaction space 20 are indicated by dashed lines which end at the arrows assigned to the individual blowing levels corresponding to lines or nozzles.
  • This additional supply of heat favors the reaction of the carbon of the particles located in the after-reaction space with the likewise supplied via feed line 21 - e.g. B. -C0 2 - and steam amount to form CO and H 2 .
  • This gasification reaction consumes heat, so that in the course of the upward movement of the gas mixture, the temperature of the gas mixture is reduced again. It is then, as soon as the temperature reduction has exceeded a certain level - in which in Fig. 1 the drawing illustrated embodiment when reaching a temperature of about 1050 ° C - through the supply lines 23, 25, 27 again exothermic and endothermic gasifying agent in the post-reaction chamber 20 in the blowing levels 23a, 25a, 27a, wherein the reaction sequence described occurs.
  • a quenching agent is introduced via lines 40 in the level 40a into the post-reaction space, which lowers the temperature of the gas by approximately 80 to 100 ° C., in order to ensure that the gas mixture leaving the reactor does not contain any solid particles contains, whose ashes have softened and could cause caking in the downstream lines.
  • the amount of solid carbon in the after-reaction space 20 decreases from bottom to top, so that consequently fewer gasifying agents are required for the conversion from bottom to top. This is taken into account in the exemplary embodiment according to FIG. 1 in that the distances between the blowing levels 21a, 23a, 25a and 27a increase from the bottom up.
  • the temperature inside the fluidized bed 115 is substantially lower than that according to FIG. 1. It is between approximately 700 and 800 ° C.
  • the addition of exothermic gasifying agent is immediately above the upper limit 116 of the fluidized bed 115 to be dimensioned in the blowing-in plane 121a in such a way that the gas and solid mixture flowing out of the fluidized bed experiences a noticeable increase in temperature in the lower section, which reaches the upper temperature of the lower section, which extends from peak 130 to peak 136, at a temperature of 1100 ° C.
  • the subsequent mode of operation corresponds up to the blowing-in level 127a, ie up to the peak 136, in principle that of the exemplary embodiment according to FIG.
  • the fine grain separated from the product gas which normally still contains carbon, is returned to the fluidized bed, ie to the reactor, in addition to the carbon freshly introduced into the reactor.
  • the blowing in of the endothermally reacting gasification agent along the longitudinal axis of the after-reaction space depends on the desired uniform conversion at a uniform temperature profile. It is the case that, depending on the concentration of the carbon-containing material in the post-reaction space, only a more or less large part of the endothermic gasification agent blown into the lower blowing-in region is converted, so that the ratio between exothermic and endothermic reacting amounts of gasification agent remains constant or can also increase.
  • the injection areas in the post-reaction space can be arranged at the same distance from one another. The temperature profile resulting from this procedure gives a uniform sawtooth-like up and down of the temperature over the length of the after-reaction space.
  • the procedure described above is possible in connection with the exemplary embodiment shown in FIG. 3 of the drawing.
  • the temperature in the fluidized bed 215 corresponds approximately to that of the exemplary embodiment according to FIG. 1, although that according to FIG. 2 is also possible.
  • the blow-in areas 221 to 227 are arranged at constant intervals. In all blowing levels 221a to 227a, the exothermic and endothermic gasifying agents are blown in at constant ratios to one another and, if appropriate, also in constant amounts. The latter would mean that equal amounts of endothermic and exothermic gasifying agents are blown in from all the blowing areas from bottom to top.
  • a quenching agent can be supplied via a feed line 240.
  • Solid particles should be managed in such a way that heat consumption and heat supply correspond to each other in such a way that a constant temperature level is maintained in the individual sections or - more precisely - the temperature within the post-reaction space or the sections over its or its axial extent by an average value only slightly varied on both sides, the maximum temperature occurring possibly being just below the temperature limit at which softening the ash particles to difficulties, i. H. could lead to caking or formation of larger agglomerates.
  • the temperature profile is idealized in all the figures of the drawing.
  • the crucial point is that the temperature fluctuations around an average temperature, which in turn can fluctuate to a small extent, are kept as small as possible, and the amplitude does not have to be constant over the entire length of the after-reaction space. Rather, it can fluctuate within limits along the reactor axis, that is, it can become larger or smaller.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP80107380A 1979-12-08 1980-11-26 Procédé de fonctionnement d'un réacteur à lit fluidisé pour gazéifier des matières carbonacées Expired EP0030323B1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE19792949533 DE2949533A1 (de) 1979-12-08 1979-12-08 Verfahren zum betreiben eines wirbelbettreaktors zum vergasen von kohlenstoffhaltigem material
DE2949533 1979-12-08
DE3033115 1980-09-03
DE19803033115 DE3033115A1 (de) 1980-09-03 1980-09-03 Verfahren zum betreiben eines wirbelbettreaktors zum vergasen von kohlenstoffhaltigem material

Publications (2)

Publication Number Publication Date
EP0030323A1 true EP0030323A1 (fr) 1981-06-17
EP0030323B1 EP0030323B1 (fr) 1986-05-07

Family

ID=25782316

Family Applications (1)

Application Number Title Priority Date Filing Date
EP80107380A Expired EP0030323B1 (fr) 1979-12-08 1980-11-26 Procédé de fonctionnement d'un réacteur à lit fluidisé pour gazéifier des matières carbonacées

Country Status (7)

Country Link
EP (1) EP0030323B1 (fr)
AU (1) AU536933B2 (fr)
BR (1) BR8008022A (fr)
DD (1) DD155174A1 (fr)
DE (1) DE3071595D1 (fr)
GR (1) GR71896B (fr)
TR (1) TR21877A (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0634470A1 (fr) * 1993-07-12 1995-01-18 M. W. Kellogg Company Gazéificateur à lit entraîné
EP0726307A1 (fr) * 1995-02-13 1996-08-14 Thermoselect Aktiengesellschaft Procédé pour éliminer des substances organiques nocives dans le gaz de synthèse produit par la gazeification de déchets municipaux
WO2007090585A1 (fr) * 2006-02-06 2007-08-16 Rwe Power Aktiengesellschaft Procede et reacteur de gazeification avec extraction du laitier liquide
CN110591762A (zh) * 2019-09-16 2019-12-20 中国科学院工程热物理研究所 循环流化床气化装置和循环流化床气化方法
CN118599561A (zh) * 2024-08-06 2024-09-06 广东以色列理工学院 一种多段控温防止热载体团聚的林木废料热解方法和装置

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4340459C1 (de) * 1993-11-27 1995-05-18 Rheinische Braunkohlenw Ag Verfahren zum Betreiben eines Wirbelschichtreaktors zum Vergasen von kohlenstoffhaltigen Einsatzstoffen
DE19548324C2 (de) * 1994-12-23 1998-08-06 Rheinische Braunkohlenw Ag Verfahren zum Vergasen von kohlenstoffhaltigen Feststoffen in der Wirbelschicht sowie dafür verwendbarer Vergaser
DE102007006980B4 (de) * 2007-02-07 2009-03-19 Technische Universität Bergakademie Freiberg Verfahren zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2643298A1 (de) * 1976-09-25 1978-04-06 Davy Bamag Gmbh Verfahren zur kontinuierlichen vergasung von feinteiligem, kohlenstoffhaltigem material

Family Cites Families (6)

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Publication number Priority date Publication date Assignee Title
US1913968A (en) * 1928-02-09 1933-06-13 Ig Farbenindustrie Ag Fuel gas
US2558746A (en) * 1948-02-10 1951-07-03 Texas Co Production of carbon monoxide and other gases from carbonaceous materials
DE937486C (de) * 1949-09-08 1956-01-05 Rudolf Dr-Ing Drawe Verfahren und Gaserzeuger zur Vergasung staubfoermiger oder feinkoerniger Brennstoffe
US3840353A (en) * 1971-07-30 1974-10-08 A Squires Process for gasifying granulated carbonaceous fuel
DE2741805A1 (de) * 1977-09-16 1979-03-29 Rheinische Braunkohlenw Ag Verfahren und vorrichtung zum vergasen von festem, kohlenstoffhaltigem material
DE2801574B1 (de) * 1978-01-14 1978-12-21 Davy Powergas Gmbh, 5000 Koeln Wirbelschichtschachtgenerator zum Vergasen feinkörniger Brennstoffe

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2643298A1 (de) * 1976-09-25 1978-04-06 Davy Bamag Gmbh Verfahren zur kontinuierlichen vergasung von feinteiligem, kohlenstoffhaltigem material

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0634470A1 (fr) * 1993-07-12 1995-01-18 M. W. Kellogg Company Gazéificateur à lit entraîné
EP0726307A1 (fr) * 1995-02-13 1996-08-14 Thermoselect Aktiengesellschaft Procédé pour éliminer des substances organiques nocives dans le gaz de synthèse produit par la gazeification de déchets municipaux
WO2007090585A1 (fr) * 2006-02-06 2007-08-16 Rwe Power Aktiengesellschaft Procede et reacteur de gazeification avec extraction du laitier liquide
CN110591762A (zh) * 2019-09-16 2019-12-20 中国科学院工程热物理研究所 循环流化床气化装置和循环流化床气化方法
CN118599561A (zh) * 2024-08-06 2024-09-06 广东以色列理工学院 一种多段控温防止热载体团聚的林木废料热解方法和装置

Also Published As

Publication number Publication date
DE3071595D1 (en) 1986-06-12
AU536933B2 (en) 1984-05-31
TR21877A (tr) 1987-02-13
DD155174A1 (de) 1982-05-19
GR71896B (fr) 1983-08-10
BR8008022A (pt) 1981-06-23
EP0030323B1 (fr) 1986-05-07
AU6511580A (en) 1981-06-18

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