EP0148799A2 - Verfahren zur Vergasung von Kohle und Schlämmen - Google Patents

Verfahren zur Vergasung von Kohle und Schlämmen Download PDF

Info

Publication number
EP0148799A2
EP0148799A2 EP85400018A EP85400018A EP0148799A2 EP 0148799 A2 EP0148799 A2 EP 0148799A2 EP 85400018 A EP85400018 A EP 85400018A EP 85400018 A EP85400018 A EP 85400018A EP 0148799 A2 EP0148799 A2 EP 0148799A2
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
schlamms
fines
coal
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.)
Granted
Application number
EP85400018A
Other languages
English (en)
French (fr)
Other versions
EP0148799B1 (de
EP0148799A3 (en
Inventor
Serge Delessard
Pierre Henri Sagnier
Pierre Etienne André Palat
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.)
Charbonnages de France CDF
Original Assignee
Charbonnages de France CDF
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 Charbonnages de France CDF filed Critical Charbonnages de France CDF
Publication of EP0148799A2 publication Critical patent/EP0148799A2/de
Publication of EP0148799A3 publication Critical patent/EP0148799A3/fr
Application granted granted Critical
Publication of EP0148799B1 publication Critical patent/EP0148799B1/de
Expired legal-status Critical Current

Links

Images

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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J2300/0956—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
    • C10J2300/0959—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
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam

Definitions

  • the present invention relates to a process for the gasification of coal schlamms in gasification plants in an ash agglomeration fluidized bed.
  • These installations include a reactor in which the coal is maintained in a fluidized bed at a temperature of approximately 900 to 1100 ° C. by injection of water vapor and oxygen at the base of the reactor. Under these conditions, the coal gasifies, while the ash particles formed undergo a start of softening and stick to each other, forming agglomerates. The ashes are separated by a selective withdrawal made possible by the difference in size and density between these agglomerates, on the one hand, and the particles still containing carbon, on the other hand, which are not agglomerated. In the installations which are the subject of the cited patents, the separation takes place in one or more venturis located at the base of the reactor.
  • the fluidizing gas is steam and for oxygen to be injected at high speed, mixed with steam, by a tube. located in the center of the venturi, while a gas mainly consisting of water vapor is introduced by the venturi.
  • the jet thus formed in the bed constitutes a hot zone which plays a decisive role in the process of agglomeration of the ash particles.
  • the gases entrain a large quantity of fines constituted, on the one hand, by particles of non-carbonated carbon or incompletely gasified, on the other hand, by ash.
  • These fines are separated, preferably in cyclones, and recycled to the base of the gasification reactor.
  • the flow of fines which is thus continuously recycled is high, for example of the order of 5 times the flow of coal to be gasified.
  • the carbonating carbon is preferably introduced into the upper zone of the fluidized bed, by pneumatic transport, after having been ground to a particle size less than or equal to 6 mm and optionally dried so that its moisture content does not exceed 6%. It may even suffer, as described in US Patent No. 4,057,402, pretreatment at about 400 ° C, so as to reduce its agglutinating properties.
  • German patent N ° 497,894 Even if the process which is the subject of this patent takes advantage of the high temperature of the gases leaving the reactor to achieve partial drying up to about 10% of water and preheating of the product to be gasified, none remains not least that the risks of agglutination and clogging are prohibitive, since the product to be gasified is introduced entirely into the flow leaving the reactor. It is symptomatic to note that, although this patent is very old, the mode of injection which it describes has never been used effectively in the industrial processes which appeared later including in the process developed by the inventors mentioned in this German patent.
  • the schlamms are a by-product of coal preparation plants which are obtained in large quantities in coal wash houses and which cannot be satisfactorily recovered.
  • An object of the present invention is to allow the development of schlamms by gasifying them simultaneously with coal used as main raw material.
  • Another object of the invention is to carry out the gasification of schlamms in an installation such as that which is the subject of European patent application N'0.027.280.
  • a third object of the invention is to take advantage of the latent heat of the products obtained in a gasification reaction in a fluidized bed to dry slurries so as to introduce them in the practically dry state into the lower zone of a fluidized bed.
  • coal gasification By practically dry schlamms is meant a product whose water content is less than 6% by weight and preferably less than 2 to 3% by weight.
  • An additional object of the invention is to dilute the schlamms in the products which are recycled to the gasification reactor, so as to avoid the risks of agglutination and clogging in the injection conduits and to allow this injection without the correct operation of the gasification reactor is disturbed.
  • the invention therefore consists of an improvement to a gasification process in which carbonated carbon is introduced directly into a fluidized bed; oxygen and water vapor are blown into the lower part of the fluidized bed; the ashes are collected in the molten state at the base of the fluidized bed; the products leaving the fluidized bed are successively directed to one or more separation devices for fines and gases and the fines are recycled in the fluidized bed.
  • This improvement consists in injecting schlamms into the circuit of the products which leave the fluidized bed and in introducing the mixture of the dried schlamms and fines separated from the gases in the fluidized bed, preferably directly in the lower part thereof.
  • the schlamms are introduced directly into the gasification reactor, inside the gas phase which overcomes the fluidized bed (disengagement zone).
  • the schlamms are introduced into the flow of hot gases leaving the reactor and before the introduction of this flow into the separation and recycling cycle of the fines.
  • the schlamms are introduced into the circuit or circuits for recycling the fines between the outlet of the separation station (s) for these fines and the reactor.
  • the general reference 1 designates the gasification reactor produced in a manner known per se which it is not necessary to describe here operating in a fluidized bed at a temperature of approximately 900 to 1100 °. C, coal being admitted in 2 and steam and air or oxygen maintaining the fluidization being, respectively, introduced in 3 and 4 at the base of the reactor.
  • the ash particles of the coal thus treated undergo an initial softening and stick together to form agglomerates.
  • Selective removal of the ash is based on the difference in size and density between these agglomerates, on the one hand, and the particles still containing carbon which are not agglomerated, on the other hand.
  • the separation takes place in 5 at the base of the reactor and the products are drawn off in 6.
  • the gases resulting from this treatment and which are charged with a large proportion of water vapor and fines with a particle size less than 1 mm are evacuated at 7, at the head of the reactor at a temperature of the order of 1000 ° C. to be admitted, with a view to the separation of these fines, into one or more cyclones such as 8-9.
  • These fines are generally recycled in the reactor 1, respectively, through the conduits 8a-9a. The fraction which would not be recycled could be withdrawn in 10.
  • the schlamms which represent a particle size fraction between 0 and 1 mm are introduced into this gaseous effluent circuit.
  • the schlamms which represent a particle size fraction between 0 and 1 mm are introduced into this gaseous effluent circuit.
  • the schlamms are admitted at 11 into the duct 7 connecting the upper part of the reactor 1 to the first cyclone 8.
  • the schlamms are brought to the temperature of the gas flow and of the fines which circulate there (of the order of 1000 ° C.) to be separated, like these fines, in the cyclone 8 and to be recycled also like the latter, at the same temperature (of the order of 850-900 ° C.) and at the degree of humidity normally prevailing in the recycling duct 8a.
  • the schlamms thus identifying with the fines both in terms of their particle size and the temperature and humidity conditions, it will be understood that they behave like the fines as well when they are admitted to the bottom of the reactor 1 that during their stay in this reactor leading to their gasification without modifying the operating conditions of the installation compared to the case where the schlamms have not been introduced into the fine circuit.
  • full advantage is taken of the sensible heat of the gases leaving the reactor.
  • these schlamms can be introduced into the recycling conduit of one of the cyclones (8-9) in which the conditions of temperature, flow rate and degree of humidity would be the most favorable.
  • we will preferably choose the pipe 8a connected to the first cyclone 8 in which the temperature is the highest (850-900 ° C).
  • we can also admit schlamms in the conduits 9a for the return of fines from cyclone 9 in which the temperature is still around 750-800 ° C (lower than that of conduit 8a) and the flow rate obviously lower to that in conduit 8a.
  • the point of admission thus depends as seen from the number of cyclones and the temperature and flow conditions.
  • the sensible heat leaving the reactor since the sensible heat leaving the reactor is not taken full advantage of, it may be advantageous to at least partially dry the slabs before their introduction into the conduit. In any event, it is advantageous to take advantage of points in the installation where these parameters have optimal values, in particular the temperature.
  • the proportion of schlamms admitted will be eminently a function of the proportion of fines recycled (proportion which is important as indicated above). This proportion may be, depending on the case, of the order of 20 / and up to 50% by weight of the quantity of carbonated carbon.

Landscapes

  • 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)
  • Industrial Gases (AREA)
EP19850400018 1984-01-10 1985-01-07 Verfahren zur Vergasung von Kohle und Schlämmen Expired EP0148799B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8400285A FR2557885B1 (fr) 1984-01-10 1984-01-10 Procede pour la gazeification de schlamms
FR8400285 1984-01-10

Publications (3)

Publication Number Publication Date
EP0148799A2 true EP0148799A2 (de) 1985-07-17
EP0148799A3 EP0148799A3 (en) 1986-06-11
EP0148799B1 EP0148799B1 (de) 1989-05-24

Family

ID=9299969

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19850400018 Expired EP0148799B1 (de) 1984-01-10 1985-01-07 Verfahren zur Vergasung von Kohle und Schlämmen

Country Status (5)

Country Link
EP (1) EP0148799B1 (de)
CN (1) CN85101391A (de)
DE (1) DE3570453D1 (de)
FR (1) FR2557885B1 (de)
IN (1) IN163507B (de)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2593496A1 (fr) * 1986-01-30 1987-07-31 Korf Engineering Gmbh Procede de gazeification des boues de curage
EP0708168A1 (de) * 1994-10-17 1996-04-24 N.V. Kema Methode und Vorrichtung zum Vergasen von festem Brennstoff
CN103881782A (zh) * 2014-04-09 2014-06-25 河南理工大学 流化床气化炉飞灰颗粒剂及其加工方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8172164B2 (en) * 2009-02-27 2012-05-08 General Electric Company Method and apparatus for a feed into a gasifier utilizing a slurry

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1074803B (de) * 1960-02-04 Badische Anilin- &. Soda-Fabrik Aktiengesellschaft, Ludwigshafen/Rhein Verfahren zur Brenngaserzeugung durch Vergasen feinzerteilter fester oder flüssiger Brennstoffe und/oder durch Spalten gasförmiger Brennstoffe in einer Wirbelschicht
DE497894C (de) * 1930-05-15 I G Farbenindustrie Akt Ges Verfahren zum Herstellen von Wassergas und anderen brennbaren Gasen
GB401463A (en) * 1932-09-01 1933-11-16 Ig Farbenindustrie Ag Improvements in and apparatus for the gasification of finelygrained moist fuels
GB1558996A (en) * 1976-07-27 1980-01-09 Gulf Oil Corp Fliud bed gasifier
US4315758A (en) * 1979-10-15 1982-02-16 Institute Of Gas Technology Process for the production of fuel gas from coal
DE3004111A1 (de) * 1980-02-05 1981-08-13 Hölter, Heinz, Ing.(grad.), 4390 Gladbeck Verfahren und vorrichtung zur durchfuehrung des verfahrens - integrierte kohle-muell-vergasung mit nachgeschalteter wirbelbettsystemtechnik
JPS5776088A (en) * 1980-10-31 1982-05-12 Nippon Kokan Kk <Nkk> Coal gasification using powdered coal and its device

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2593496A1 (fr) * 1986-01-30 1987-07-31 Korf Engineering Gmbh Procede de gazeification des boues de curage
GB2185970A (en) * 1986-01-30 1987-08-05 Korf Engineering Gmbh Process for the gasification of sewage sludge
GB2185970B (en) * 1986-01-30 1990-03-21 Korf Engineering Gmbh Process for the gasification of sewage sludge
EP0708168A1 (de) * 1994-10-17 1996-04-24 N.V. Kema Methode und Vorrichtung zum Vergasen von festem Brennstoff
CN103881782A (zh) * 2014-04-09 2014-06-25 河南理工大学 流化床气化炉飞灰颗粒剂及其加工方法

Also Published As

Publication number Publication date
EP0148799B1 (de) 1989-05-24
FR2557885A1 (fr) 1985-07-12
FR2557885B1 (fr) 1987-07-17
DE3570453D1 (en) 1989-06-29
IN163507B (de) 1988-10-01
EP0148799A3 (en) 1986-06-11
CN85101391A (zh) 1987-01-31

Similar Documents

Publication Publication Date Title
EP0161970B1 (de) Verfahren und Anlage zur Materialbehandlung in einer zirkulierenden Wirbelschicht
US3957459A (en) Coal gasification ash removal system
US4002438A (en) Organic conversion system
CA2857269C (fr) Procede de combustion en boucle chimique avec elimination en phase diluee des cendres et fines dans la zone d&#39;oxydation et installation utilisant un tel procede
EP2633003B1 (de) Herstellung von synthesegas durch erhitzung einer oxidierten biomasse mit einem aus der oxidierung von restprodukten gewonnenen heissgas
EP0173782B1 (de) Verfahren zur Behandlung von Materialen
EP0027280B1 (de) Verfahren und Vorrichtung zur Umwandlung von agglomerierfähigem, festem kohlenwasserstoffhaltigem Material in ein wertvolleres gasförmiges Produkt
CA2850612C (fr) Procede de combustion en boucle chimique avec elimination des cendres et fines en sortie de la zone d&#39;oxydation et installation utilisant un tel procede
AU2011336788A1 (en) Method and apparatus for particle recycling in multiphase chemical reactors
FR2473552A1 (fr) Procede de production de fer reduit directement avec gazeification de charbon en lit fluidise
FR2483258A1 (fr) Procede d&#39;elimination de dechets solides
EP1449907A1 (de) Anlage und Verfahren zur Vergasung einer organischen Stoff enthaltenden Ladung
US3847566A (en) Fluidized bed gasification process with reduction of fines entrainment by utilizing a separate transfer line burner stage
EP0148799B1 (de) Verfahren zur Vergasung von Kohle und Schlämmen
EP3390585B1 (de) Verfahren zur wirbelbettvergasung von reifen
EP1137591B1 (de) Teiloxidationsverfahren mit rückgewinnung von russfiltermassen
FR2546288A1 (fr) Procede de recuperation de chaleur a partir de gaz contenant des substances contaminant les surfaces de transfert de chaleur
US20260022298A1 (en) Process and process plant for converting feedstock comprising a carbon-containing solid fuel
FR2505808A1 (fr) Preparation de gaz de synthese a partir d&#39;hydrocarbures riches en cendre
GB2102831A (en) Fluidized bed gasification of coal
FR2535017A1 (fr) Procede pour la combustion du coke present sur des particules solides et pour la production de chaleur recuperable a partir de particules contenant des hydrocarbures et appareil pour la mise en oeuvre de ce procede
AU2006211317B2 (en) Apparatus and method for gasifying solid fuel
JPS5884890A (ja) タ−ルの注入でガスへのダスト同伴を抑制するロ−タリ−キルン石炭ガス発生器
FR2683829A1 (fr) Installation de traitement de reduction du minerai de fer en lit fluidise circulant.
FR2529221A1 (fr) Procede et appareil de gazeification utilisant du charbon, du coke ou une matiere du meme genre

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): BE DE FR GB NL SE

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Kind code of ref document: A3

Designated state(s): BE DE FR GB NL SE

17P Request for examination filed

Effective date: 19861127

17Q First examination report despatched

Effective date: 19871015

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE FR GB NL SE

REF Corresponds to:

Ref document number: 3570453

Country of ref document: DE

Date of ref document: 19890629

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19891231

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19900122

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19900125

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19900213

Year of fee payment: 6

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19900801

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19901129

Year of fee payment: 7

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19910107

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19910108

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Effective date: 19910131

GBPC Gb: european patent ceased through non-payment of renewal fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19911001

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Effective date: 19920930

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

EUG Se: european patent has lapsed

Ref document number: 85400018.9

Effective date: 19910910