SE453776B - WANTED TO DISPOSE WASTE FOR THE formation of a leaching-resistant slag and a gas containing only H? 712 AND CO AS FLAMMABLE INGREDIENTS - Google Patents

WANTED TO DISPOSE WASTE FOR THE formation of a leaching-resistant slag and a gas containing only H? 712 AND CO AS FLAMMABLE INGREDIENTS

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Publication number
SE453776B
SE453776B SE8502165A SE8502165A SE453776B SE 453776 B SE453776 B SE 453776B SE 8502165 A SE8502165 A SE 8502165A SE 8502165 A SE8502165 A SE 8502165A SE 453776 B SE453776 B SE 453776B
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SE
Sweden
Prior art keywords
gas
post
reaction chamber
shaft
lime
Prior art date
Application number
SE8502165A
Other languages
Swedish (sv)
Other versions
SE8502165L (en
SE8502165D0 (en
Inventor
S Santen
S Eriksson
L Bentell
H Johansson
Original Assignee
Skf Steel Eng Ab
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 Skf Steel Eng Ab filed Critical Skf Steel Eng Ab
Publication of SE8502165D0 publication Critical patent/SE8502165D0/en
Priority to DE19863611429 priority Critical patent/DE3611429A1/en
Priority to AT0090986A priority patent/AT396880B/en
Priority to DK156686A priority patent/DK166517C/en
Priority to NO861346A priority patent/NO161759C/en
Priority to NZ215734A priority patent/NZ215734A/en
Priority to IL78448A priority patent/IL78448A0/en
Priority to NL8600881A priority patent/NL8600881A/en
Priority to AU55774/86A priority patent/AU585332B2/en
Priority to US06/849,656 priority patent/US4718362A/en
Priority to CA000506240A priority patent/CA1270405A/en
Priority to ZA862683A priority patent/ZA862683B/en
Priority to GB08608887A priority patent/GB2174691B/en
Priority to IT20054/86A priority patent/IT1188649B/en
Priority to ES554119A priority patent/ES8704614A1/en
Priority to JP61090177A priority patent/JPH0649186B2/en
Priority to FR868606183A priority patent/FR2581380B1/en
Priority to FI861794A priority patent/FI861794A/en
Priority to BE0/216608A priority patent/BE904705A/en
Publication of SE8502165L publication Critical patent/SE8502165L/en
Publication of SE453776B publication Critical patent/SE453776B/en

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8668—Removing organic compounds not provided for in B01D53/8603 - B01D53/8665
    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/08—Continuous processes with ash-removal in liquid state
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/14—Continuous processes using gaseous heat-carriers
    • 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
    • C10K3/006—Reducing the tar content by steam reforming
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F23G5/0276—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using direct heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/085—High-temperature heating means, e.g. plasma, for partly melting the waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/24—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a vertical, substantially cylindrical, combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/301—Treating pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/104—Combustion in two or more stages with ash melting stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/20—Supplementary heating arrangements using electric energy
    • F23G2204/201—Plasma
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/60—Sorption with dry devices, e.g. beds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y02E50/14—

Description

15 20 25 453 776 bildade gasen inmatas i en efterreaktionskammare under samtidig energitillförsel med en het, plasmagenerator- upphettad gas för att i närvaro av vattenånga termiskt reformera i gasen ingående kolväten till CO och H2. The gas formed in the gas is fed into a post-reaction chamber during simultaneous energy supply with a hot, plasma generator-heated gas to thermally reform in the presence of water vapor in the gas hydrocarbons to CO and H2.

Den i schaktugnen genererade gasen innehåller föroreningar bl.a. i form av tunga kolväten. Genom energitillförseln i efterreaktionskamwuen och närvaron av vatten som för- àngats från avfallsmaterialet, spjälkas kolvätena termiskt till 'co och H2.The gas generated in the shaft furnace contains pollutants, e.g. in the form of heavy hydrocarbons. Due to the energy supply in the post-reaction chamber and the presence of water evaporated from the waste material, the hydrocarbons are thermally cleaved to 'co and H2.

Enligt en utföringsform av uppfinningen utnyttjas plasma- generatorupphettad oxiderande gas, företrädesvis luft, för energitillförseln i schaktugnens nedre del. Härigenom kan temperaturen styras noggrant och snabbt till önskad nivå alltefter variationerna i avfallets sammansättning.According to an embodiment of the invention, plasma generator heated oxidizing gas, preferably air, is used for the energy supply in the lower part of the shaft furnace. In this way, the temperature can be controlled accurately and quickly to the desired level according to the variations in the composition of the waste.

Genom att utnyttja en plasmagenerator för upphettning av gasen, kan den heta gasen ges en mycket hög energi- täthet och härigenom blir den tillförda gasvolymen för den erforderliga energimängden förhållandevis mycket liten.By using a plasma generator for heating the gas, the hot gas can be given a very high energy density and thereby the supplied gas volume for the required amount of energy becomes relatively very small.

Enligt en annan utföringsform av uppfinningen injiceras dessutom finfördelad koks och/eller vattenånga i efter- reaktionskammaren för att kompensera för ett för lågt C- och/eller H20-innehåll.According to another embodiment of the invention, in addition, atomized coke and / or water vapor is injected into the post-reaction chamber to compensate for a too low C and / or H 2 O content.

Enlnfizen anmæzutföringsform av uppfinningen underkastas gasen-dessutom ett katalytiskt reningssteg för att avlägs- na eventuella rester av tyngre kolväten. Härvid leds gasen genom en kammare innehållande en katalysator. Kata- lysatorn är företrädesvis kalk eller dolomit, men även andra katalysatorer är tänkbara, exempelvis nickel.According to one embodiment of the invention, the gas is additionally subjected to a catalytic purification step to remove any residues of heavier hydrocarbons. In this case, the gas is passed through a chamber containing a catalyst. The catalyst is preferably lime or dolomite, but other catalysts are also conceivable, for example nickel.

Processen styres företrädesvis så att temperaturen i 10 15 20 25 30 453 776 den från schaktugnen utgående gasen uppgår till högst 800°C och så att temperaturen i den från efterreaktions- kammaren kommande gasblandningen överstiger l00O°C, och företrädesvis uppgår till cirka l200°C. Den höga tempera- turen i efterreaktionskammaren ger en väsentligen full- ständig, termisk sönderdelning av i gasen förekommande tunga kolväten.The process is preferably controlled so that the temperature of the gas leaving the shaft furnace amounts to at most 800 ° C and so that the temperature of the gas mixture coming from the post-reaction chamber exceeds 100 ° C, and preferably amounts to about 1200 ° C. . The high temperature in the post-reaction chamber results in a substantially complete, thermal decomposition of heavy hydrocarbons present in the gas.

I schaktets nedre del upprätthàlles en temperatur som överstiger slaggens smältpunkt. Vid slaggens stelnande glasas i slaggen förekommande, icke förgasningsbara be- ståndsdelar in, vilket sedan möjliggör en säker depone- ring av slaggen.In the lower part of the shaft a temperature is maintained which exceeds the melting point of the slag. During the solidification of the slag, non-gasifiable constituents present in the slag are glazed in, which then enables a safe disposal of the slag.

Enligt ytterligare en annan utföringsform av uppfinningen genomföres också en rening med avseende pà i gasen före- kommande klorföreningar, genom att gasen efter kylning genom värmeväxling leds genom en kammare innehållande bränd kalk. Den brända kalken kan härvid med fördel häm- tas frán ett tidigare katalytiskt reningssteg, i vilket kalksten/dolomit kalcinerats pà grund av gasens höga ingàngstemperatur.According to yet another embodiment of the invention, a purification is also carried out with respect to chlorine compounds present in the gas, in that the gas, after cooling by heat exchange, is passed through a chamber containing burnt lime. The burnt lime can be advantageously recovered from a previous catalytic purification step, in which limestone / dolomite has been calcined due to the high inlet temperature of the gas.

Ytterligare fördelar och kännetecken hos uppfinningen kommer att framgå av nedanstående detaljerade beskrivning i anslutning till bifogade ritning, pà vilken fig. 1 visar en schematisk vy av en anläggning för genomförande av processen enligt uppfinningen, och fig. 2 visar en anordning för katalytisk sönderdel- ning av tunga kolväten och avlägsnande av klor- föreningar ur den vid avfallspyrolysen genere- rade gasen. 10 15 20 25 30 453 776 Avfallsmaterialet inmatas i en med l betecknad schakt- ugn genom en lämplig slussanordning 2. Energi och oxi- dationsmedel tillföres i schaktugnens nedre del, i det visade utförandet medelst en eller flera anordningar 3, 4 för tillförsel av het luft. Dessa anordningar kan till exempel utgöras av plasmageneratorer. Den vid pyrolysen genererade gasen avdrages via en ringtrumma 5, som i det visade utförandet är sä anordnad, att gas- en avdrages under nivån för avfallsmaterialets 6 över- yta 7 i schaktugnen.Further advantages and features of the invention will become apparent from the following detailed description taken in conjunction with the accompanying drawing, in which Fig. 1 shows a schematic view of a plant for carrying out the process according to the invention, and Fig. 2 shows a catalytic decomposition device. of heavy hydrocarbons and removal of chlorine compounds from the gas generated in the waste pyrolysis. 10 15 20 25 30 453 776 The waste material is fed into a shaft furnace designated by 1 through a suitable locking device 2. Energy and oxidizing agents are supplied in the lower part of the shaft furnace, in the embodiment shown by means of one or more devices 3, 4 for supplying hot air. These devices can be, for example, plasma generators. The gas generated during the pyrolysis is drawn off via an annular drum 5, which in the embodiment shown is arranged so that the gas is drawn off below the level of the surface 7 of the waste material 6 in the shaft furnace.

Den så genererade gasen inledes härefter i en efterreak- tionskammare 8. Energi tillföres medelst en het gas, som i det visade föredragna utförandet upphettas i en plasmagenerator 9. Härvid kan gasen helt eller delvis ledes genom plasmageneratorn. Vidare kan vid behov fin- fördelad koks och/eller vattenånga tillföras genom lan- sar 10 i anslutning till inloppet ll för den glasmagene- ratorupphettade gasen. I efterreaktionskammaren uppnås en termisk sönderdelning av i gasen förekommande föro- reningar i form av främst tyngre kolväten.The gas thus generated is then introduced into a post-reaction chamber 8. Energy is supplied by means of a hot gas, which in the preferred embodiment shown is heated in a plasma generator 9. In this case, the gas can be passed in whole or in part through the plasma generator. Furthermore, if necessary, finely divided coke and / or water vapor can be supplied through lances 10 in connection with the inlet 11 for the glass generator heated gas. In the post-reaction chamber, a thermal decomposition of contaminants present in the gas is achieved in the form of mainly heavier hydrocarbons.

Efter denna termiska sönderdelning kan gasen underkastas ytterligare rening i en anordning 12, vilket endast sche- matiskt antydes pà ritningen i form av en tom kammare.After this thermal decomposition, the gas can be subjected to further purification in a device 12, which is only schematically indicated in the drawing in the form of an empty chamber.

Sålunda kan i nämnda kammare injiceras finfördelad kalk för katalytisk sönderdelning av eventuellt i gasen kvar- varande tunga kolväten. Alternativt kan gasen ledas genom en fyllning av styckeformig kalk eller en annan katalysa- tor för sönderdelningsprocessen.Thus, finely divided lime can be injected into said chamber for catalytic decomposition of any heavy hydrocarbons remaining in the gas. Alternatively, the gas can be passed through a filling of lumpy lime or another catalyst for the decomposition process.

/J Härefter kan gasen underkastas klorreningssteg, se när- mare beskrivningen i anslutning till fig. 2, och sedan i ett avslutande steg befrias från kvicksilver genom utkondensering av detta. 10 15 20 25 30 453 776 Gasreningsutrustningen enligt fig. 2 innefattar ett förs- ta schakt 13 innehållande en kalkstens- eller dolomitfyll- ning 14, vilken inmatas i schaktet genom en gastät sluss- anordning 15. Gasen från efterreaktionskammaren inmatas efter en eventuell värmeväxling genom ett gasinlopp 16 vid schaktets botten och avdrages efter passage genom fyllningen genom ett gasutlopp 17 vid schaktets topp./ J Thereafter, the gas can be subjected to chlorine purification steps, see the description in more detail in connection with Fig. 2, and then in a final step freed from mercury by condensing it. The gas purification equipment according to Fig. 2 comprises a first shaft 13 containing a limestone or dolomite filling 14, which is fed into the shaft through a gas-tight sluice device 15. The gas from the post-reaction chamber is fed after a possible heat exchange through a gas inlet 16 at the bottom of the shaft and is deducted after passage through the filling through a gas outlet 17 at the top of the shaft.

I schaktets botten är anordnat ett utmatningsbord eller ' motsvarande för utmatning av helt eller delvis kalcine- rad kalksten genom en gastät slussanordning 18.At the bottom of the shaft a discharge table or the like is arranged for discharging wholly or partly calcined limestone through a gas-tight lock device 18.

Den utmatade, helt eller delvis kalcinerade kalkstenen transporteras därefter på transportband eller liknande, i figuren antytt med ledningen 19, till ett andra med 20 betecknat schakt genom en gastät slussanordning 21 till bildning av en fyllning 22.The discharged, fully or partially calcined limestone is then transported on conveyor belts or the like, in the figure indicated by the line 19, to a second shaft designated 20 by a gas-tight lock device 21 to form a filling 22.

Den fràn schaktet 13 utmatade gasen matas genom en ledning 23 till en värmeväxlare 24 och värmeväxlas företrädesvis med luft, varigenom gasens fysiska värme kan tas tillvara för utnyttjande vid tidigare processteg eller för andra ändamål. Gasen leds därefter genom ledningen 25 till ett nedre gasinlopp 26 i det andra schaktet och leds genom fyllningen 22 för att sedan avdragas genom ett vid schaktets 20 topp beläget gasutlopp 27. I schaktets bot- ten är anordnat ett utmatningsbord eller liknande för utmatning av den vid klorreningen bildade produkten ge- nom en gastät slussanordning 28.The gas discharged from the shaft 13 is fed through a line 23 to a heat exchanger 24 and is preferably heat exchanged with air, whereby the physical heat of the gas can be utilized for utilization in previous process steps or for other purposes. The gas is then led through the line 25 to a lower gas inlet 26 in the second shaft and is led through the filling 22 to then be drawn off through a gas outlet 27 located at the top of the shaft 20. A discharge table or the like is arranged in the bottom of the shaft for discharging it at the chlorine ring formed the product through a gas-tight lock device 28.

Gasen, som inleds i botten av det första schaktet, skall uppvisa en temperatur överstigande cirka 800°C. Vid dessa temperaturer kalcineras kalkstenen under bildning av CaO + C02 eller liknande, spjälkas med hjälp av H20 och/eller C02 . Gasens innehåll av tunga kolvägen, såsom tjäror med CaO som katalysator. Kalkstenskvaliteten väljes i be- roende av den rådande gastemperaturen, eftersom olika typer 10 15 20 25 453 776 av kalksten kalcineras vid olika temperaturer. I detta första steg fungerar kalken således endast som kataly- sator vid spjälkningen och påverkas icke av gasens kemis- ka sammansättning. Den utmatade, kalcinerade kalkstenen uppvisar också styckeform men är nu mycket porös.The gas, which starts at the bottom of the first shaft, should have a temperature exceeding about 800 ° C. At these temperatures the limestone is calcined to form CaO + CO 2 or similar, decomposed with H 2 O and / or CO 2. The content of the gas in the heavy carbon pathway, such as tar with CaO as catalyst. The limestone quality is chosen depending on the prevailing gas temperature, since different types of limestone are calcined at different temperatures. In this first step, the lime thus only functions as a catalyst during the decomposition and is not affected by the chemical composition of the gas. The discharged, calcined limestone also has a piece shape but is now very porous.

Sedan tjärorna eller de tunga kolvätena i gasen avlägsnats kan gasen utan problem värmeväxlas. Företrädesvis värme- växlas gasen med kall luft och den värmda luften kan sedan utnyttjas vid något eller några av de föregående processtegen.After the tar or heavy hydrocarbons in the gas have been removed, the gas can be heat exchanged without any problems. Preferably, the gas is heat exchanged with cold air and the heated air can then be used in one or more of the previous process steps.

Den kalcinerade kalkstenen transporteras vidare till det andra schaktet och bildar i detta en fyllning, som utnyttjas för rening av gasen från innehâllna klorföre- ningar och/eller klor. Härvid sker till exempel reaktion- erna Ca0 + 2HCl till bildning av CaCl2. Denna reaktion bör ske under smältpunkten för CaCl2 i föreliggande form.The calcined limestone is transported further to the second shaft and forms in it a filling, which is used for purifying the gas from the chlorine compounds and / or chlorine contained. In this case, for example, the reactions CaO + 2HCl take place to form CaCl2. This reaction should occur below the melting point of CaCl 2 in the present form.

Den avgående gasen är därmed befriad från kolväteförening- ar och klorföreningar och efter eventuell utkondensering av kvicksilver kommer gasen att som brännbara bestånds- delar enbart innehålla CO och H2, och efter en förbränning kan gasen som då enbart innehåller C02, H20 och N2, släppas ut i atmosfären.The exhaust gas is thus freed from hydrocarbon compounds and chlorine compounds and after any condensation of mercury, the gas will contain as combustible constituents only CO and H2, and after a combustion the gas which then only contains CO2, H2O and N2 can be emitted. in the atmosphere.

Genom att utnyttja sättet enligt föreliggande uppfinning kan sålunda alla de skadliga, miljöfarliga ämnen, som normalt förorsakar stora problem vid konventionella, i dag utnyttjade processer, tas om hand och omvandlas till-ofarliga och eventuellt också användbara produkter, såsom CaCl2. fw ff)Thus, by utilizing the method of the present invention, all the harmful, environmentally hazardous substances which normally cause major problems in conventional, currently utilized processes can be disposed of and converted into harmless and possibly also useful products, such as CaCl 2. fw ff)

Claims (10)

10 15 20 25 453 776 P a t e n t k r a v10 15 20 25 453 776 P a t e n t k r a v 1. l. Sätt att destruera avfall till bildning av en laknings- beständig slagg och en gas som enbart innehåller H2 och CO som brännbara beståndsdelar, enligt vilket avfallsmaterial inmatas från toppen av en schaktugn under samtidig energi- tillförsel medelst het oxiderande gas vid schaktugnens bot- ten, flytande slagg utmatas från schaktugnens botten och bildad, bland annat tyngre kolväten innehållande gas, av- drages från schaktets övre del, k ä n n e t e c k n a t av att den vid pyrolys av avfallsmaterialet bildade gasen inmatas i en efterreaktionskammare under samtidig energi- tillförsel med en het, plasmageneratorupphettad gas för att i närvaro av vattenånga termiskt reformera i gasen ingåen- de kolväten till CO och H2.1. l. Method of destroying waste to form a leach-resistant slag and a gas containing only H2 and CO as combustible constituents, according to which waste material is fed from the top of a shaft furnace during simultaneous energy supply by hot oxidizing gas at the bottom of the shaft furnace liquid slag is discharged from the bottom of the shaft furnace and formed, including heavier hydrocarbons containing gas, is withdrawn from the upper part of the shaft, characterized in that the gas formed during pyrolysis of the waste material is fed into a post-reaction chamber with simultaneous energy supply with a hot, plasma generator heated gas to thermally reform the hydrocarbons to CO and H2 in the presence of water vapor into the gas. 2. Sätt enligt krav l, k ä n n e t e c k n a t av att den i efterreaktíonskammaren tillförda heta gasen utgöres av luft, recirkulerad gas eller kvävgas.2. A method according to claim 1, characterized in that the hot gas supplied to the post-reaction chamber consists of air, recycled gas or nitrogen gas. 3. Sätt enligt krav 1 - 2, k ä n n e t e c k n a t av att vattenånga injiceras i efterreaktionskammaren.3. A method according to claims 1 - 2, characterized in that water vapor is injected into the post-reaction chamber. 4. Sätt enligt krav l - 3, k ä n n e t e c k n a t av att finfördelad koks injiceras i efterreaktionskammaren.4. A method according to claims 1-3, characterized in that atomized coke is injected into the post-reaction chamber. 5. Sätt enligt krav l - 4, k ä n n e t e c k n a t av att gasen från efterreaktionskammaren i ett ytterligare steg underkastas katalytisk rening.5. A method according to claims 1-4, characterized in that the gas from the post-reaction chamber is subjected to catalytic purification in a further step. 6. Sätt enligt krav 5, k ä n n e t e c k n a t av att gasen leds genom en fyllning av styckformiq kalk.6. A method according to claim 5, characterized in that the gas is passed through a filling of piece-shaped lime. 7. Sätt enligt krav 5, k ä n n e t e c k n a t av att pulverformig kalk injiceras i gasen. 10 453 7767. A method according to claim 5, characterized in that powdered lime is injected into the gas. 10 453 776 8. Sätt enligt krav l - 7, k ä n n e t e c k n a t av att i gasen eventuellt förekommande klorföreningar spjäl- kas genom att gasen leds genom en kammare innehållande gen fyllning av bränd kalk.8. A method according to claims 1-7, characterized in that any chlorine compounds present in the gas are decomposed by passing the gas through a chamber containing a refill of burnt lime. 9. Sätt enligt krav 6 och 8, k ä n n e t e'c k n a t av att vid spjälkningen utnyttjas vid katalytisk sönderdel- ning bildad bränd kalk.9. A method according to claims 6 and 8, characterized in that burnt lime formed during catalytic decomposition is used in the cleavage. 10.- Sätt enligt krav l - 9, k ä n n e t e c k n a t av att den i efterreaktionskammaren tillförda energimängden styrs så att den i efterreaktionskammaren genererade gas- blandningen uppvisar en temperatur överstigande cirka 1ooo°c.10. A method according to claims 1 - 9, characterized in that the amount of energy supplied in the post-reaction chamber is controlled so that the gas mixture generated in the post-reaction chamber has a temperature exceeding about 1 000 ° C.
SE8502165A 1985-02-15 1985-05-03 WANTED TO DISPOSE WASTE FOR THE formation of a leaching-resistant slag and a gas containing only H? 712 AND CO AS FLAMMABLE INGREDIENTS SE453776B (en)

Priority Applications (18)

Application Number Priority Date Filing Date Title
DE19863611429 DE3611429A1 (en) 1985-02-15 1986-04-05 WASTE DECOMPOSITION METHOD
AT0090986A AT396880B (en) 1985-05-03 1986-04-07 WASTE DECOMPOSITION METHOD
DK156686A DK166517C (en) 1985-05-03 1986-04-07 WASTE DISPOSAL PROCEDURES
NO861346A NO161759C (en) 1985-05-03 1986-04-07 PROCEDURE FOR DISPOSAL OF WASTE.
NZ215734A NZ215734A (en) 1985-05-03 1986-04-08 Destroying waste to form slag and combustible gas
IL78448A IL78448A0 (en) 1985-05-03 1986-04-08 Waste destruction method
NL8600881A NL8600881A (en) 1985-02-15 1986-04-08 WASTE DESTRUCTION.
CA000506240A CA1270405A (en) 1985-05-03 1986-04-09 Waste destruction
US06/849,656 US4718362A (en) 1985-02-15 1986-04-09 Waste destruction
AU55774/86A AU585332B2 (en) 1985-05-03 1986-04-09 Waste destruction
ZA862683A ZA862683B (en) 1985-05-03 1986-04-10 Waste destruction
GB08608887A GB2174691B (en) 1985-02-15 1986-04-11 Waste destruction
IT20054/86A IT1188649B (en) 1985-05-03 1986-04-11 DESTRUCTION OF WASTE
ES554119A ES8704614A1 (en) 1985-05-03 1986-04-17 Method of decomposing and treating waste
JP61090177A JPH0649186B2 (en) 1985-05-03 1986-04-21 Waste decomposition method
FR868606183A FR2581380B1 (en) 1985-02-15 1986-04-29 WASTE DESTRUCTION
FI861794A FI861794A (en) 1985-05-03 1986-04-29 AVFALLSDESTRUKTION.
BE0/216608A BE904705A (en) 1985-02-15 1986-04-30 DESTRUCTION OF WASTE.

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
SE8500755A SE452560B (en) 1985-02-15 1985-02-15 Domestic and industrial waste disposal

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SE8502165D0 SE8502165D0 (en) 1985-05-03
SE8502165L SE8502165L (en) 1986-08-16
SE453776B true SE453776B (en) 1988-02-29

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SE8502165A SE453776B (en) 1985-02-15 1985-05-03 WANTED TO DISPOSE WASTE FOR THE formation of a leaching-resistant slag and a gas containing only H? 712 AND CO AS FLAMMABLE INGREDIENTS

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SE462630B (en) * 1988-03-16 1990-07-30 Flaekt Ab PROCEDURE AND DEVICE FOR RECOVERY OF ENERGY IN METALLURGICAL PROCESSES

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SE8502165L (en) 1986-08-16
SE452560B (en) 1987-12-07
SE8502165D0 (en) 1985-05-03
SE8500755D0 (en) 1985-02-15
SE8500755L (en) 1986-08-16

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