WO1994009087A1 - Procede de fabrication et d'epuration de gaz combustibles - Google Patents

Procede de fabrication et d'epuration de gaz combustibles Download PDF

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Publication number
WO1994009087A1
WO1994009087A1 PCT/AT1993/000157 AT9300157W WO9409087A1 WO 1994009087 A1 WO1994009087 A1 WO 1994009087A1 AT 9300157 W AT9300157 W AT 9300157W WO 9409087 A1 WO9409087 A1 WO 9409087A1
Authority
WO
WIPO (PCT)
Prior art keywords
coke
gas
inert gas
reactor
coke bed
Prior art date
Application number
PCT/AT1993/000157
Other languages
German (de)
English (en)
Inventor
Wolfgang Nieder
Manfred Winkler
Leo Seirlehner
Gerhard Perchtold
Original Assignee
Austrian Industries Aktiengesellschaft
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 Austrian Industries Aktiengesellschaft filed Critical Austrian Industries Aktiengesellschaft
Priority to EP93924421A priority Critical patent/EP0620840B1/fr
Priority to DE59305263T priority patent/DE59305263D1/de
Publication of WO1994009087A1 publication Critical patent/WO1994009087A1/fr

Links

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
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • 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 method for producing and cleaning combustible gases from exhaust gases from a pyrolysis plant or a smelting reactor, in which the exhaust gas is passed over a coke bed.
  • the invention now aims to provide a method of the type mentioned, which enables direct use of the latent heat contained in the process exhaust gases from pyrolysis plants or melting processes and at the same time enables conversion in a thermoreactor with which a particularly high-quality export gas can be achieved can.
  • the method according to the invention essentially consists in preheating the coke fed to the coke bed to temperatures of> 600 ° C. with a heated inert gas.
  • a coke bed preheated with a heated inert gas is used ensures that the subsequent gasification process in the thermoreactor is under-stoichiometrically controlled and the exhaust gas is enriched with carbon monoxide and hydrogen.
  • thermoreactor with such a preheated coke bed, organic substances contained in the exhaust gas, such as hydrocarbons, are split in a reducing atmosphere and, due to the substoichiometric gasification with constant carbon specification, the exhaust gas is enriched with combustible gases.
  • the exhaust gas is enriched with combustible gases.
  • the heated coke is adjusted to a reduced slag melting temperature by adding lime and optionally further additives, the energy expenditure is further reduced and a direct energy-optimized recycling of coke ash achieved to slag, which can be used directly as a resource in the construction and / or cement industry.
  • the minimum melting temperatures achieved in this way for the slag resulting from the ash entry also leads to a Energy-efficient extremely inexpensive disposal of pollutants, such as sulfur, where appropriate, further additives, such as lime in particular, and preferably in an amount sufficient for the desulfurization of the export gas can be added.
  • the preheating of the coke is carried out by circulating inert gas, the inert gas being heated in a heat exchanger by the hot export gas leaving the coke bed reactor to temperatures of over 650 ° C., in particular about 730 ° C. .
  • inert gas serves primarily to reliably prevent premature ignition and to ensure the substoichiometric reaction conditions during the reaction in the thermoreactor.
  • the preheating is done by indirect heat exchange via a gas / gas heat exchanger.
  • the CO content of the circulated inert gas is monitored and, if a limit value of inert gas, in particular N 2 , is exceeded, the excess gas cycle quantity which reaches the coke bed generator is regulated. Overall, particularly small amounts of gas are thereby achieved, which also further reduces the technical outlay for downstream gas cleaning stages.
  • the procedure is such that the export gas is passed over a hot gas cyclone and that the separated dust is returned to the reactor, with the dust discharged from the preheating shaft of the coke also advantageously being at least 50% by weight, preferably about 70% % By weight, separated and returned to the coke bed reactor becomes.
  • the reaction of the exhaust gases in the coke bed results in a gas enriched with CO and H 2 in the case of understoichiometric C-fix gasification, which has heating values between 2.5 kwh. ⁇ r 3 n to 3.5 kwh.m " 3 n results.
  • the preheating of the coke in a separate preheating shaft enables the coke consumption in the coke bed reactor to be reduced. Naturally, the remaining portion of the sensible heat contained in the export gas can still be used separately for generating process steam.
  • An oxygen return can be provided in the lower area of the coke bed reactor, where at the same time coke ash and aggregates are melted to form a slag which can be used as a valuable substance after subsequent quenching and granulation.
  • the coke heated in a preheating shaft can be fed into the coke bed reactor via a cellular wheel sluice.
  • the regulation of the CO content already mentioned at the outset can be carried out in a particularly simple manner in such a way that when the CO content increases, an inert gas flushing gas is introduced into the Preheating cycle takes place. Due to the pressure increase associated with this, a valve can be opened with which a partial flow for pressure equalization of the inert gas circulation system is diverted into the coke bed reactor.
  • thermoreactor 1 denotes a preheated coke bed containing a thermoreactor, to which 2 exhaust gases are fed to an upstream pyrolysis plant or a melting reactor (not shown).
  • the CO and H 2 -containing waste gas which is produced, for example, in the pyrolysis of waste in a preceding process is essentially only subjected to dust separation, for example in a hot gas cyclone, before being introduced into the thermoreactor.
  • the coke bed located in the thermoreactor 1 is preheated to a temperature of about 730 ° C. using an inert gas circuit described in more detail below, and is introduced into the thermoreactor 1 via a cellular wheel sluice 3 at 4.
  • lime and possibly other additives are added to the coke in order to achieve a reduced slag melting temperature.
  • the combustible gas flowing through the coke bed in the thermoreactor and supplied via line 2 is further enriched with carbon monoxide and hydrogen in a substoichiometric C-fix gasification process to increase its calorific value, the chemical reactions listed below primarily taking place in the coke bed reactor.
  • C + CO 2 2CO (Boudouard)
  • C + 2H 2 CH 4 (methanization)
  • C + H 2 O CO + H 2 (heterogeneous water gas reaction)
  • thermoreactor 1 The combustible gas cleaned in the thermoreactor 1 and having an increased calorific value by enrichment with - CO and H 2 is withdrawn from the thermoreactor 1 at 5 and fed to a hot cyclone 6, the dust separated in the hot cyclone 6 in turn passing into the thermoreactor 7 is returned.
  • the exhaust gas is also desulphurized.
  • the sulfur separated from the process gas is bound in the slag 9.
  • the resulting slag leaves the coke bed reactor, is quenched and granulated.
  • the combustible gas or export gas enriched with CO and H 2 at temperatures of about 1000 ° C. reaches a heat exchanger 10 in which the sensible thermal energy contained in the combustible gas is partly used to heat the coke Transfer used inert gas
  • the combustible gas passes through a further heat exchanger 11 and through a waste heat boiler 12, the temperature in the waste heat boiler being reduced to approximately 250 ° C. with the generation of steam 13.
  • the combustible gas is discharged via a line 14 5 and fed to a cleaning system or a further use.
  • a preheating shaft 15 is used, through which an inert gas, such as nitrogen, flows from bottom to top.
  • Coke 18 and the additives 19 mentioned above, such as lime in particular, are fed to the preheating shaft via a cellular wheel sluice 16 via line 17.
  • the inert gas used to preheat the coke enters the preheating shaft 15 at 20 and leaves it via a line 21, enters a dust filter 22 and, after compression in a compressor 23, passes through the heat exchanger 10, in which in countercurrent to the from the Hot gas cyclone 6 discharged combustible gas, the inert gas is heated to a temperature of approximately 750 ° C., so that the coke in the preheating shaft 15 has a temperature of approximately 730 ° C. immediately before entering the thermoreactor 1.
  • the dust filter 22 serves to separate the solids, which are carried away by the gas phase when the coke layer flows through the preheating shaft 15, dusting of about 2% of the coke input being expected.
  • the dust or solid withdrawn from the dust filter 22 via a lock 24 at 25 is returned to the thermoreactor 1 together with air or nitrogen supplied via a line 26.
  • the CO concentration in the inert gas circuit or nitrogen circuit is continuously monitored, as is indicated by the measuring device or the sensor 27. If the CO content is increased above a predetermined limit, the supply of fresh inert gas, such as nitrogen, via line 28 reduces the CO concentration.
  • control lines 29, a control device 30 and a corresponding valve circuit 31 are indicated.
  • a valve 34 is actuated via a control unit 32 and control lines 33, so that over a branch line 35 after the blower 23 a corresponding partial flow of the gas in the inert gas circuit is fed directly into the thermoreactor 1 after passing through the heat exchanger 11, so that the pressure i inert gas circuit for preheating the coke to be introduced into the thermoreactor 1 is kept constant.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Processing Of Solid Wastes (AREA)
  • Furnace Details (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)

Abstract

Dans un procédé de fabrication et d'épuration de gaz combustibles provenant des gaz brûlés (2) d'une installation pyrolytique ou d'un réacteur de fusion, selon lequel les gaz brûlés (2) sont passés au-dessus d'un lit de coke (1), le coke amené jusqu'au lit de coke (1) est préchauffé à des températures de plus de 600 °C au moyen d'un gaz inerte chauffé. Ce procédé permet d'utiliser directement la chaleur contenue dans les gaz brûlés de traitement se dégageant d'installations pyrolytiques ou de processus de fusion, ainsi que d'obtenir, par transformation dans un réacteur thermique, un gaz de sortie facilement réutilisable.
PCT/AT1993/000157 1992-10-19 1993-10-19 Procede de fabrication et d'epuration de gaz combustibles WO1994009087A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP93924421A EP0620840B1 (fr) 1992-10-19 1993-10-19 Procede de fabrication et d'epuration de gaz combustibles
DE59305263T DE59305263D1 (de) 1992-10-19 1993-10-19 Verfahren zur herstellung und reinigung brennbarer gase

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA2061/92 1992-10-19
AT206192A AT399509B (de) 1992-10-19 1992-10-19 Verfahren zur herstellung und reinigung brennbarer gase

Publications (1)

Publication Number Publication Date
WO1994009087A1 true WO1994009087A1 (fr) 1994-04-28

Family

ID=3526949

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AT1993/000157 WO1994009087A1 (fr) 1992-10-19 1993-10-19 Procede de fabrication et d'epuration de gaz combustibles

Country Status (5)

Country Link
EP (1) EP0620840B1 (fr)
JP (1) JP2701984B2 (fr)
AT (1) AT399509B (fr)
DE (1) DE59305263D1 (fr)
WO (1) WO1994009087A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0025205A1 (fr) * 1979-09-04 1981-03-18 HERKO Pyrolyse GmbH & Co. Recycling KG Procédé de fabrication de gaz permanents et de suie à partir de déchets et réacteur de craquage pour la mise en oeuvre de ce procédé
EP0152912A2 (fr) * 1984-02-22 1985-08-28 Kraftwerk Union-Umwelttechnik GmbH Procédé pour la production de gaz combustibles à partir de déchets
EP0203430A1 (fr) * 1985-05-07 1986-12-03 Phoenix Gesellschaft für Rauchgasreinigung und Umwelttechnik mbH Procédé d'épuration des gaz de fumée et installation pour sa mise en oeuvre

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0025205A1 (fr) * 1979-09-04 1981-03-18 HERKO Pyrolyse GmbH & Co. Recycling KG Procédé de fabrication de gaz permanents et de suie à partir de déchets et réacteur de craquage pour la mise en oeuvre de ce procédé
EP0152912A2 (fr) * 1984-02-22 1985-08-28 Kraftwerk Union-Umwelttechnik GmbH Procédé pour la production de gaz combustibles à partir de déchets
EP0203430A1 (fr) * 1985-05-07 1986-12-03 Phoenix Gesellschaft für Rauchgasreinigung und Umwelttechnik mbH Procédé d'épuration des gaz de fumée et installation pour sa mise en oeuvre

Also Published As

Publication number Publication date
DE59305263D1 (de) 1997-03-06
EP0620840B1 (fr) 1997-01-22
EP0620840A1 (fr) 1994-10-26
JP2701984B2 (ja) 1998-01-21
AT399509B (de) 1995-05-26
JPH07502781A (ja) 1995-03-23
ATA206192A (de) 1994-10-15

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