DK169057B1 - Process for the transfer of solid, almost anhydrous glass waste and plants for carrying out the process - Google Patents
Process for the transfer of solid, almost anhydrous glass waste and plants for carrying out the process Download PDFInfo
- Publication number
- DK169057B1 DK169057B1 DK441489A DK441489A DK169057B1 DK 169057 B1 DK169057 B1 DK 169057B1 DK 441489 A DK441489 A DK 441489A DK 441489 A DK441489 A DK 441489A DK 169057 B1 DK169057 B1 DK 169057B1
- Authority
- DK
- Denmark
- Prior art keywords
- gas
- mass
- waste gas
- glass
- waste
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims description 52
- 230000008569 process Effects 0.000 title claims description 33
- 239000007787 solid Substances 0.000 title claims description 12
- 239000010922 glass waste Substances 0.000 title claims description 3
- 238000012546 transfer Methods 0.000 title description 4
- 239000002912 waste gas Substances 0.000 claims description 116
- 239000007789 gas Substances 0.000 claims description 99
- 238000002844 melting Methods 0.000 claims description 91
- 230000008018 melting Effects 0.000 claims description 91
- 239000011521 glass Substances 0.000 claims description 80
- 239000000156 glass melt Substances 0.000 claims description 47
- 238000004140 cleaning Methods 0.000 claims description 22
- 239000007859 condensation product Substances 0.000 claims description 22
- 210000000941 bile Anatomy 0.000 claims description 20
- 239000000654 additive Substances 0.000 claims description 18
- 239000002699 waste material Substances 0.000 claims description 18
- 238000000746 purification Methods 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 13
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 12
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 11
- 239000000155 melt Substances 0.000 claims description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M sodium chloride Inorganic materials [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 8
- 238000005406 washing Methods 0.000 claims description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 7
- 239000003513 alkali Substances 0.000 claims description 7
- 229910052799 carbon Inorganic materials 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 6
- 239000012080 ambient air Substances 0.000 claims description 6
- 235000011132 calcium sulphate Nutrition 0.000 claims description 6
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 238000000605 extraction Methods 0.000 claims description 6
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims description 6
- 235000019341 magnesium sulphate Nutrition 0.000 claims description 6
- 239000003507 refrigerant Substances 0.000 claims description 6
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 5
- 230000000996 additive effect Effects 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 239000010802 sludge Substances 0.000 claims description 5
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 5
- 235000011152 sodium sulphate Nutrition 0.000 claims description 5
- 238000004056 waste incineration Methods 0.000 claims description 5
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 claims description 4
- 239000002826 coolant Substances 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 4
- 239000001175 calcium sulphate Substances 0.000 claims description 3
- 238000010309 melting process Methods 0.000 claims description 3
- 239000004576 sand Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical class [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 2
- 239000001110 calcium chloride Substances 0.000 claims description 2
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 2
- 235000011148 calcium chloride Nutrition 0.000 claims description 2
- 229910052681 coesite Inorganic materials 0.000 claims description 2
- 229910052906 cristobalite Inorganic materials 0.000 claims description 2
- 230000007812 deficiency Effects 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Inorganic materials [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 claims description 2
- INHCSSUBVCNVSK-UHFFFAOYSA-L lithium sulfate Inorganic materials [Li+].[Li+].[O-]S([O-])(=O)=O INHCSSUBVCNVSK-UHFFFAOYSA-L 0.000 claims description 2
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 2
- 238000005259 measurement Methods 0.000 claims description 2
- 238000005192 partition Methods 0.000 claims description 2
- 229910052700 potassium Inorganic materials 0.000 claims description 2
- 239000011591 potassium Substances 0.000 claims description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M potassium chloride Inorganic materials [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 2
- 235000011164 potassium chloride Nutrition 0.000 claims description 2
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 claims description 2
- 229910052939 potassium sulfate Inorganic materials 0.000 claims description 2
- 235000011151 potassium sulphates Nutrition 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 239000000377 silicon dioxide Substances 0.000 claims description 2
- 235000012239 silicon dioxide Nutrition 0.000 claims description 2
- 229910052682 stishovite Inorganic materials 0.000 claims description 2
- 238000005496 tempering Methods 0.000 claims description 2
- RBTVSNLYYIMMKS-UHFFFAOYSA-N tert-butyl 3-aminoazetidine-1-carboxylate;hydrochloride Chemical compound Cl.CC(C)(C)OC(=O)N1CC(N)C1 RBTVSNLYYIMMKS-UHFFFAOYSA-N 0.000 claims description 2
- 229910052905 tridymite Inorganic materials 0.000 claims description 2
- 238000009434 installation Methods 0.000 claims 17
- 230000000737 periodic effect Effects 0.000 claims 2
- 238000005266 casting Methods 0.000 claims 1
- 238000010494 dissociation reaction Methods 0.000 claims 1
- 230000005593 dissociations Effects 0.000 claims 1
- 159000000011 group IA salts Chemical class 0.000 claims 1
- 229910001385 heavy metal Inorganic materials 0.000 description 14
- 150000002013 dioxins Chemical class 0.000 description 11
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 10
- 150000001805 chlorine compounds Chemical class 0.000 description 10
- 150000002240 furans Chemical class 0.000 description 10
- 239000002956 ash Substances 0.000 description 7
- 230000006378 damage Effects 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000003570 air Substances 0.000 description 4
- 229910052783 alkali metal Inorganic materials 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000010276 construction Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 239000003517 fume Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000006060 molten glass Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 3
- 229910052753 mercury Inorganic materials 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 150000001447 alkali salts Chemical class 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 239000004566 building material Substances 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- -1 chlorine hydrogen Chemical class 0.000 description 2
- 239000010849 combustible waste Substances 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000011819 refractory material Substances 0.000 description 2
- 238000009877 rendering Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- 241000237858 Gastropoda Species 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 210000000013 bile duct Anatomy 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 150000004820 halides Chemical class 0.000 description 1
- 239000013056 hazardous product Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 235000015243 ice cream Nutrition 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000002901 radioactive waste Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000028327 secretion Effects 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 229910052718 tin Inorganic materials 0.000 description 1
- 239000011135 tin Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000010891 toxic waste Substances 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C03—GLASS; MINERAL OR SLAG WOOL
- C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
- C03B3/00—Charging the melting furnaces
- C03B3/02—Charging the melting furnaces combined with preheating, premelting or pretreating the glass-making ingredients, pellets or cullet
- C03B3/023—Preheating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/20—Agglomeration, binding or encapsulation of solid waste
- B09B3/25—Agglomeration, binding or encapsulation of solid waste using mineral binders or matrix
- B09B3/29—Agglomeration, binding or encapsulation of solid waste using mineral binders or matrix involving a melting or softening step
-
- C—CHEMISTRY; METALLURGY
- C03—GLASS; MINERAL OR SLAG WOOL
- C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
- C03B19/00—Other methods of shaping glass
- C03B19/10—Forming beads
- C03B19/109—Glass-melting furnaces specially adapted for making beads
-
- C—CHEMISTRY; METALLURGY
- C03—GLASS; MINERAL OR SLAG WOOL
- C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
- C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
- C03B5/005—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture of glass-forming waste materials
-
- C—CHEMISTRY; METALLURGY
- C03—GLASS; MINERAL OR SLAG WOOL
- C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
- C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
- C03B5/02—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture in electric furnaces, e.g. by dielectric heating
- C03B5/027—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture in electric furnaces, e.g. by dielectric heating by passing an electric current between electrodes immersed in the glass bath, i.e. by direct resistance heating
- C03B5/03—Tank furnaces
-
- C—CHEMISTRY; METALLURGY
- C03—GLASS; MINERAL OR SLAG WOOL
- C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
- C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
- C03B5/04—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture in tank furnaces
-
- C—CHEMISTRY; METALLURGY
- C03—GLASS; MINERAL OR SLAG WOOL
- C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
- C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
- C03B5/16—Special features of the melting process; Auxiliary means specially adapted for glass-melting furnaces
- C03B5/235—Heating the glass
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
- F01N2550/00—Monitoring or diagnosing the deterioration of exhaust systems
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/50—Glass production, e.g. reusing waste heat during processing or shaping
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Glass Melting And Manufacturing (AREA)
Description
- i - DK 169057 B1- i - DK 169057 B1
Opfindelsen angår en fremgangsmåde ifølge indledningen til krav 1. Desuden angår opfindelsen et anlæg til udøvelses af fremgangsmåden.The invention relates to a method according to the preamble of claim 1. In addition, the invention relates to a plant for carrying out the method.
Det har gennem lang tid været kendt at overføre toksiske og radioaktive affaldsstoffer i form af slam og suspensioner til glas efter 5 tilsætning af tilsætningsstoffer og blanding til en masse, i hvilket glas de tidligere frit forhåndenværende skadestoffer er fast indkapslet. Glas har her den gunstige egenskab, at det er meget vanskeligt udvaskeligt, således at en frigørelse af tungmetaller og andre i glasset indeholdte materialer kun kan optræde i så lille form, at en deponering ίο eller anvendelse af legemer af et sådant glas uden videre er mulig. Sådanne fremgangsmåder er fx. kendt fra DE-patentskrift 26 31 220 eller US-patentskrift 4 666 490.It has been known for a long time to transfer toxic and radioactive waste in the form of sludge and suspensions to glass after the addition of additives and mixture to a mass in which glass the previously freely available pollutants are firmly encapsulated. Glass has the advantageous feature here that it is very difficult to wash out, so that the release of heavy metals and other materials contained in the glass can only occur in such a small form that a deposit or use of such a glass is readily possible. . Such methods are e.g. known from DE patent 26 31 220 or US patent 4 666 490.
Endvidere kendes der fra DE-offentliggørelsesskrift 31 01 455 en fremgangsmåde og et anlæg til overføring af farligt materiale til en is relativt harmløs tilstand. Der anvendes til dette formål et lukket omformningskammer, i hvilket et glasbad holdes i smeltet tilstand ved hjælp af elektrisk opvarmning. Brændbart affald indføres gennem en indløbsende i omformningskammeret og antændes og forbrændes under tilstedeværelse af tilført luft eller ilt under dannelse af gasformede 20 forbrændingsprodukter og aske. Hoveddelen af asken falder på det smeltede glas og opløses deri. Den finere askedel, som strømmer bort med det gasformede produkt, opfanges i filtre og føres tilbage til det smeltede gals, i hvilket den ligeledes opløses. Det smeltede glas udledes efter behov og køles og erstattes af friskt glas eller 25 glasbestanddele.Furthermore, from DE Publication 31 31455 a method and a plant for transferring hazardous material to an ice-cream are relatively harmless. For this purpose, a closed conversion chamber is used in which a glass bath is kept in the molten state by means of electric heating. Combustible waste is introduced through an inlet end into the conversion chamber and ignited and incinerated in the presence of supplied air or oxygen to form gaseous combustion products and ash. The bulk of the ash falls on the molten glass and dissolves therein. The finer ash flowing away with the gaseous product is trapped in filters and returned to the molten bile in which it is also dissolved. The molten glass is discharged as required and cooled and replaced by fresh glass or 25 glass ingredients.
En vanskelighed ved denne overførsel af affaldsstoffer til glasform består i, at sådanne affaldsstoffer i almindelighed indeholder en stor mængde chlorider og kalciumsulfat, der ved smeltningen kun i ringe omfang optages af glassmelten, også når optageevnen for glassmelten for 30 chlorider og svovl udnyttes indtil mætningsgrænsen, da den til smeltning bestemte masse indeholder tilsvarende meget af det. Dette fører uhensigtsmæssigt til, at store spildgasmængder fremkommer med gasser stammende fra chlorider og sulfater, især Cl, HC1, SO. og SO . I mod-sætning hertil optages tungmetaller ganske vist i tilstrækkeligt omfang 35 i glasset, men det er en ulempe, at de opstående spildgasser alligevel - 2 - DK 169057 B1 indeholder tungmetaller samt yderligere alkalimængder, som undviger ved fordampning fra glassmelten. Den tungest vejende ulempe ved den kendte fremgangsmåde, især i retning af dens miljøvenlighed, er den, at der ved opvarmningen af massen under smeltningen fremkommer eller i det 5 mindste kan forekomme dannelse af dioxiner og/eller furaner, nemlig når der i de til omarbejdning bestemte affaldsstoffer dels foreligger endnu organiske bestanddele og dels tungmetaller, af hvilke der ved de under smeltningen af massen optrædende temperaturer dannes eller kan dannes de nævnte skadestoffer. Ved fremgangsmåden ifølge DE-offentliggørelses-lo skrift 31 01 455 kommer yderligere den indskrænkning, at den kun er egnet til brændbart affaldsmateriale.One difficulty with this transfer of glass wastes is that such wastes generally contain a large amount of chlorides and calcium sulphate which, when melted, is only poorly absorbed by the glass melt, even when the absorption capacity of the glass melt for 30 chlorides and sulfur is utilized up to the saturation limit. since the mass determined for melting contains similarly much of it. Consequently, large amounts of waste gas are produced with gases from chlorides and sulphates, in particular Cl, HCl, SO. and SO. In contrast, heavy metals are admittedly sufficiently 35 in the glass, but it is a disadvantage that the resulting waste gases nevertheless contain heavy metals as well as additional alkali quantities which evade from evaporation from the glass melt. The most significant disadvantage of the known process, especially in the direction of its environmental friendliness, is that during the heating of the pulp during the melting, or at least formation of dioxins and / or furans can occur, namely when in the process of reworking. certain wastes are partly still organic components and partly heavy metals, of which at the temperatures occurring during the melting of the pulp, the said harmful substances can be formed or can be formed. In addition, the method according to DE-Publication No. 31 01 455 has the restriction that it is only suitable for combustible waste material.
Der fremkommer derfor den opgave at tilvejebringe en fremgangsmåde af den indledningsvis nævnte art, som har en bedre miljøvenlighed, og som især udelukker en udledning af dioxiner og/eller furaner også ved 15 anvendelse af heterogene, organiske bestanddele samt tungmetaller indeholdende affaldsstoffer, og hvor de ved smeltningen af forbrændingsasken opstående stoffer i mindst mulig grad, om overhovedet, skal deponeres. Endvidere fremkommer den opgave at anvise et anlæg til udøvelse af fremgangsmåden.It is therefore the object of the present invention to provide a process of the kind mentioned above, which has a better environmental friendliness, and which in particular precludes the discharge of dioxins and / or furans also by the use of heterogeneous organic constituents and heavy metals containing waste materials and when the melting of the combustion box, substances arising as little as possible, if at all, must be deposited. Furthermore, the task arises to provide a plant for carrying out the method.
20 Løsningen på den første del af opgaven lykkes ifølge opfindelsen ved en fremgangsmåde af den indledningsvis nævnte art ifølge ejendommelighederne i krav 1.The solution to the first part of the task succeeds according to the invention by a method of the kind mentioned initially according to the characteristics of claim 1.
Med den nye fremgangsmåde kan et hidtil meget problematisk affaldsstof, nemlig affaldsforbrændingsaske, omarbejdes på miljøvenlig 25 måde til glas, selv om sådanne asker er sammensat heterogent med store og svingende mængder især af kulstof, kviksølv, bly, tin, zink, kalcium, chlorider og halogenider. En stor del af skadestofferne fra affaldsforbrændingsasken går umiddelbart over i glassmelten og bindes således fast. Skadestoffer, som undviger i gasform, kondenseres i vid ud-30 strækning ved afkøling inden i den til smeltning bestemte masse og føres atter til smeltetilførslen. De derpå resterende, kolde spildgasser, som nu fremkommer i relativt lille mængde, uskadeliggøres i den efterfølgende gasrensning.With the new approach, a hitherto very problematic waste material, namely waste incineration ash, can be recycled in an environmentally friendly way to glass, although such ashes are heterogeneously composed with large and fluctuating amounts especially of carbon, mercury, lead, tin, zinc, calcium, chlorides and halides. A large part of the pollutants from the waste incinerator box immediately goes into the glass melt and thus bond. Damage which is avoided in gaseous form is largely condensed by cooling within the mass determined for melting and is returned to the melt feed. The remaining cold waste gases, which now appear in relatively small quantities, are rendered harmless in the subsequent gas purification.
En videreudformning af opfindelsen foreslår, at den fra den smel-35 tende masse udtrædende, varme spildgas eftervarmes i en periode på - 3 - DK 169057 B1 mindst 1,5 sek. til en temperatur på mindst 1200°C, derpå forafkøles under delvis kondensation til en temperatur mellem 200 og 300°C, føres i tilslutning hertil ind i den til smeltning bestemte masse og afkøles der under yderligere kondensation til 20 til 50°C, og at de ved foraf-5 køling opstående kondensationsprodukter føres tilbage i den til smeltning bestemte masse og/eller udtrækkes. Ved eftervarmningen af spildgassen ødelægges her de eventuelt tilstedeværende dioxiner og/eller furaner med sikkerhed, hvorhos den mindste temperatur og opholdstid selvfølgeligt er valgt således, at denne med sikkerhed er tilstrækkelig ίο til den ønskede ødelæggelse. Den herpå udtrukne, varme spildgas indeholder da i det væsentlige kun chlorider, sulfater, kuldioxid samt alkali- og tungmetal dampe. Denne varme spildgas kondenseres delvist ved den følgende forafkøling til 200 - 300°C og reduceres dermed i sin mængde samt i antallet af indeholdte stoffer. De fremkommende kondensais tionsprodukter holdes med den foreslåede tilbageførsel i den til smeltning bestemte masse i et lukket kredsløb og overføres efterhånden til glasset, hvorhos der efter en indløbsfase opnås en ligevægtstilstand, i hvilken mængden af kondensationsprodukter forbliver i det væsentlige konstant. Ved gennemledningen af den forafkølede spildgas gennem den 20 til smeltning bestemte masse opnås det, at også dampe, som først kondenserer ved lave temperaturer, som fx. tungmetal-dampe og især kviksølvdampe, udlejres i massepartiklerne og således atter tilbageføres til smelteprocessen. På grund af den stærke afkøling af spildgassen på dens vej gennem massen udkondenseres her chlorider og sulfater praktisk 25 taget fuldstændigt. Såfremt der fordampes flere chlorider og sulfater, end der efterfølgende kan opløses i glassmelten efter tilbageførslen af de kondenserede produkter, indtræder en berigelse af disse stoffer i massen. For at undgå dette udsluses på hensigtsmæssig måde i det mindste den overskydende andel af de ved forafkølingen opstående kondensa-30 tionsprodukter. Disse kondensationsprodukter er i det væsentlige faste produkter. Den herefter resterende kolde spildgas indeholder da næsten udelukkende chlorbrinte (HC1) og svovldioxid (S02) i stor koncentration. Volumenet af den endnu resterende kolde spildgas er her relativt lille i forhold til kapaciteten af affaldsforbrændingsaske. Desuden er den 35 her foreliggende relativt store koncentration og enkle sammensætning af - 4 - DK 169057 B1 den kolde spildgas en fordel for den efterfølgende, afsluttende gasrensning. Gasrensningen fordrer kun en relativt lille kapacitet og leverer desuden forholdsvis rene udski 11 el sesprodukter, isser natriumklorid og natriumsulfat, der fx. kan anvendes til fremstillingen af soda.A further embodiment of the invention proposes that the hot waste gas emerging from the melting mass be heated for a period of at least 1.5 sec. to a temperature of at least 1200 ° C, which is then cooled under partial condensation to a temperature between 200 and 300 ° C, is subsequently fed into the melting mass and cooled to 20 to 50 ° C under further condensation and that the condensation products arising from pre-cooling are returned to the mass determined for melting and / or extracted. Here, when the waste gas is heated, any dioxins and / or furans present, with the minimum temperature and residence time, of course selected so as to be sufficiently sufficient for the desired destruction, are destroyed. The extracted hot waste gas then contains essentially only chlorides, sulphates, carbon dioxide as well as alkali and heavy metal fumes. This hot waste gas is partially condensed by the following pre-cooling to 200 - 300 ° C and is thus reduced in its quantity and in the number of substances contained. The resulting condensation products are kept with the proposed return in the melt-melted mass in a closed circuit and gradually transferred to the glass, where, after an inlet phase, an equilibrium state is obtained in which the amount of condensation products remains substantially constant. By passing the precooled waste gas through the mass determined for melting, it is also obtained that vapors which first condense at low temperatures, such as e.g. heavy metal vapors and especially mercury vapors are deposited in the pulp particles and thus returned to the melting process. Due to the strong cooling of the waste gas on its way through the mass, chlorides and sulphates are almost completely condensed here. If more chlorides and sulphates are evaporated than can subsequently be dissolved in the glass melt after the return of the condensed products, enrichment of these substances enters the mass. In order to avoid this, at least the excess proportion of the condensation products arising from the pre-cooling is extinguished. These condensation products are essentially solid products. The remaining cold waste gas then contains almost exclusively chlorine hydrogen (HCl) and sulfur dioxide (SO2) in high concentration. The volume of the remaining cold waste gas is relatively small here compared to the capacity of waste incineration ash. In addition, the relatively large concentration and simple composition of the cold waste gas present herein is an advantage for the subsequent final gas purification. The gas purification requires only a relatively small capacity and also delivers relatively clean elec- tricity products, freezing sodium chloride and sodium sulphate, for example. can be used in the manufacture of soda.
5 Den til smeltningen nødvendige varmeenergi frembringes her fortrinsvis elektrisk, da der herved undgås en den senere spildgasbehandling vanskel i ggørende ti Iblanding af forbrændingsgasser fra med fossile brændsler drevne varmebrændere ind i den fra den smeltende masse stammende spildgas.The heat energy needed for the melting is preferably electrically generated here, since this avoids the subsequent waste gas treatment difficult in making combustion gases from fossil fuel-fired heat burners into the waste gas originating from the melting mass.
ίο Den nye fremgangsmåde er i stor grad både miljøvenlig og økono misk, da den dels i vid udstrækning mindsker udledningen af spildgas og dels leverer andre værdifulde råstoffer, nemlig glaslegemer, der fx. kan anvendes som byggemateriale eller byggematerialetilsætning, og det nævnte natrium-chlorid og -sulfat. En udledning af dioxiner og/eller is furaner er udelukket ved den nye fremgangsmåde.ίο The new approach is to a large extent both environmentally friendly and economical, since it largely reduces the emission of waste gas and supplies other valuable raw materials, namely glass bodies, for example. may be used as building material or building material addition, and said sodium chloride and sulfate. An emission of dioxins and / or ice furans is excluded by the new method.
Endvidere foreslås det med fremgangsmåden, at efteropvarmningen af den varme spildgas sker i en separat efteropvarmer. Denne fremgangsmådevariant er ganske vist ikke så gunstig i retning af energibalance, men er imidlertid med et relativt lille opbud med hensyn til smelte-20 anlæg gennemførlig og byder desuden på den fordel, at hele glasbadet kan dækkes med massen, således at en stor del af alkali- og tungmetal-dampene allerede kondenserer i massedækket i smelteovnen.Furthermore, the method proposes that the post-heating of the hot waste gas takes place in a separate post-heater. Although this method variant is not so favorable in the direction of energy balance, it is, however, feasible with a relatively small supply with regard to smelting plants and also offers the advantage that the entire glass bath can be covered with the pulp, so that a large part of the the alkali and heavy metal fumes are already condensing in the pulp deck of the furnace.
En alternativ, særlig energigunstig udformning af fremgangsmåden foreslår, at glassmelten på en del af sin overflade holdes fri for 25 masse, og at den varme spildgas efter udtrædningen fra den smeltende masse ledes over den massefrie del af overfladen af glassmelten og eftervarmes ved varmeoptagelse fra glassmelten.An alternative, particularly energy-favorable design of the process proposes that the glass melt on a part of its surface be kept free of 25 mass and that the hot waste gas after the exit from the melting mass is passed over the mass-free part of the surface of the glass melt and is heated by heat absorption from the glass melt. .
En yderligere alternativ fremgangsmåde foreslår, at den fra den til smeltning bestemte masse udtrædende kolde spildgas efteropvarmes i 30 mindst 1,5 sek. til en temperatur på mindst 1200°C og derpå renses.A further alternative method proposes that the cold waste gas extracted from the mass for melting be re-heated for at least 1.5 seconds. to a temperature of at least 1200 ° C and then purified.
Også her sikres det, at dioxiner og/eller furaner ikke kommer ud i miljøet, men ødelægges ved en passende opvarmning af spildgassen.Here, too, it is ensured that dioxins and / or furans do not enter the environment, but are destroyed by adequate heating of the waste gas.
Som et sidste alternativ i retning af efteropvarmning af spildgasserne foreslår fremgangsmåden endeligt, at den rensede spildgas efter-35 opvarmes i mindst 1,5 sek. til en temperatur på mindst 1200°C. Også - 5 - DK 169057 B1 herved opnås den ønskede ødelæggelse af dioxiner og/eller furaner. Udvalget af de til anvendelse bestemte fremgangsmådevarianter ligger inden for fagmandens skøn og retter sig efter fordringerne og de foreliggende omstændigheder i det enkelte tilfælde.As a last alternative towards post-heating of the waste gases, the method finally proposes that the purified waste gas be post-heated for at least 1.5 seconds. to a temperature of at least 1200 ° C. Also, hereby the desired destruction of dioxins and / or furans is achieved. The range of process variants to be used is within the discretion of the person skilled in the art and is subject to the claims and the circumstances of each case.
5 For at forbedre varmeoverførslen fra glassmelten til den til smelt ning bestemte masse foreslås det, at der på den med masse dækkede del af overfladen af glassmelten frembringes et flydende alkalisalt- eller jordalkalisalt-gallelag, som ved behovsstyret aftrækning holdes i et lagtykkelsesområde mellem 2 og 5 cm. Foruden en fremskyndelse af smelt-lo ningen opnås en binding af en del af de fra den smeltende masse udtrædende skadestoffer i gallelaget, således at spildgassen belastes tilsvarende mindre. Den behovsstyrede, aftrukne, med skadestoffer berigede alkalisalt-galle kan efter afkøling og størkning fx. atter tilføres processen, hvorhos skadestofferne fra gal!elåget efterhånden træder 15 over i glassmelten.In order to improve the heat transfer from the glass melt to the mass determined for melting, it is proposed that on the mass-covered part of the surface of the glass melt, a liquid alkali salt or alkaline earth salt bile layer is produced which is maintained in a layer thickness range between 2 and 5 cm. In addition to accelerating the melt solution, a bonding of some of the pollutants emanating from the melting mass is obtained in the bile layer, so that the waste gas is correspondingly less loaded. The demand-controlled, drawn-out, enriched with harmful substances alkali salt bile can, for example, after cooling and solidification. The process is again applied, whereby the pollutants from the bile duct eventually enter 15 into the glass melt.
Det foretrækkes, at der som gallelag anvendes et i det væsentlige af natriumsulfat eller -chlorid eller kaliumsulfat eller -chlorid eller litiumsulfat eller -chlorid eller af en blanding af disse bestående gallelag, og at dette gallelag frembringes under smeltningen ved omsæt-20 ning fra kalciumsulfat, kalciumchlorid, magnesiumsulfat og/eller magne-siumchlorid, der tilføres smelteprocessen med affaldsforbrændingsasken og/eller som særskilt tilsætningsstof i massen. Alternativt foreslås det, at der ved høje smeltetemperaturer og/eller ved alkalimangel anvendes et kalciumsulfit- og/eller magnesiumsulfat-gallelag, og at dette 25 gallelag fremstilles umiddelbart af med massen eller som særskilt tilsætningsstof tilført kalciumsulfat og/eller magnesiumsulfat. De afholdte tilsætningsomkostninger holdes således meget lave, således at de i forhold til de ved spildgasrensningen sparede omkostninger er små. Dermed bliver fremgangsmåden som helhed økonomisk gennemførlig.It is preferred that a bile layer is used essentially of sodium sulfate or chloride or potassium sulfate or chloride or lithium sulfate or chloride or of a mixture of these existing bile layers and that this bile layer is produced during the melting by reaction from calcium sulfate , calcium chloride, magnesium sulfate, and / or magnesium chloride, which is fed to the melting process with the waste incinerator box and / or as a separate additive in the pulp. Alternatively, it is suggested that at high melting temperatures and / or in the case of alkali deficiency, a calcium sulfite and / or magnesium sulfate bile layer be used and that this bile layer be prepared directly from the pulp or as a separate additive added calcium sulfate and / or magnesium sulfate. Thus, the addition costs incurred are kept very low, so that the costs saved by the waste gas purification are small. Thus, the process as a whole becomes economically feasible.
30 Med hensyn til yderligere tilsætningsstoffer foreslår fremgangsmå den, at der anvendes Si02-holdige stoffer, især sand og/eller phonolit. Disse tilsætningsstoffer er enkle at anvende og billige. Alternativt eller kompleterende kan der også anvendes glasskår som Si02-holdigt tilsætningsstof.With respect to additional additives, the method suggests the use of SiO 2 containing substances, especially sand and / or phonolite. These additives are easy to use and inexpensive. Alternatively or in addition, glass shards can also be used as SiO2-containing additives.
35 Desuden foreslår fremgangsmåden, at den fra den smeltende masse - 6 - DK 169057 B1 udtrædende, varme spildgas bortledes og forafkøles under undertryk, at den forafkølede spildgas sættes under overtryk, og at gennemledningen af spildgassen gennem den til smeltning bestemte masse i modstrøm i forhold til denne reguleres således, at trykket af den fra den til 5 smeltning bestemte masse udtrædende kolde spildgas i det væsentlige er lig med omgivelseslufttrykket. Herved opnås der dels, at spildgas, som træder ud af den smeltende masse, på ingen måde kan komme ud i miljøet, og dels sørges der for en tilstrækkelig gennemstrømning af forafkølet spildgas gennem den til smeltning bestemte masse. Endelig bliver der ίο således endvidere opnået, at der ved massefremstillingen hverken kan komme nævneværdige mængder spildgas ud i miljøet eller falsk luft ind i spildgassen.In addition, the process proposes that the hot waste gas emerging from the melting mass is discharged and cooled under vacuum, that the pre-cooled waste gas is pressurized and that the flow of the waste gas through the melting mass is countercurrent to this it is regulated so that the pressure of the cold waste gas exiting from the mass of 5 to melt is substantially equal to the ambient air pressure. This results in part that waste gas exiting the melting mass can in no way enter the environment, and in addition, sufficient flow of pre-cooled waste gas through the mass determined for melting is provided. Finally, it is thus obtained that in the mass production neither significant quantities of waste gas can enter the environment nor false air into the waste gas.
For at holde mængden af de til deponering bestemte stoffer mindst mulig kan der til massen tilblandes støv og/eller slam fra gasrensningis en.In order to minimize the amount of the substances intended for landfill, dust and / or sludge from the gas purification can be added to the mass.
For at opnå en absolut uskadelig rengas ledes spildgassen efter gasrensning på hensigtsmæssig måde gennem et aktivt kulfilter, og for at forenkle spildgasbehandlingen kan spildgassen hensigtsmæssigt afkøles før eller efter gasrensningen.In order to obtain an absolutely harmless gas, the waste gas after gas purification is suitably passed through an active carbon filter, and to simplify the waste gas treatment, the waste gas can be suitably cooled before or after the gas purification.
20 Løsningen på den anden del af opgaven lykkes ifølge opfindelsen ved hjælp af et anlæg ifølge krav 15.The solution to the second part of the task succeeds according to the invention by means of a system according to claim 15.
Dette anlæg muliggør en sikker, kontinuerlig og miljøskånsom udøvelse af den forudbeskrevne fremgangsmåde.This plant enables safe, continuous and environmentally gentle practice of the method described above.
Hensigtsmæssige udformninger og videreudformninger af anlægget er 25 anført i de afhængige krav 16 til 32.Appropriate designs and further designs of the plant are set out in the dependent claims 16 to 32.
Udførelseseksempler for anlægget samt et forløbseksempel for fremgangsmåden forklares i det følgende ved hjælp af en tegning. På tegningen viser: 30 fig. 1 et anlæg til udøvelse af fremgangsmåden ifølge opfindel sen i skematisk snitgengivelse i en første udformning, fig. 2-4 anlægget i en ændret udformning, fig. 5 en gasrensningsindretning som en del af anlægget ifølge fig. 1 til 4 i en første udformning i skematisk blokgen-35 givel se, og - 7 - DK 169057 B1 fig. 6 gasrensningsindretningen i en anden udformning, ligeledes i skematisk blokgengivelse.Embodiment examples of the plant as well as a process example of the method are explained below by means of a drawing. In the drawing: FIG. 1 shows a system for carrying out the method according to the invention in schematic sectional representation in a first embodiment; FIG. 2-4 the plant in a modified configuration, fig. 5 shows a gas cleaning device as part of the system of FIG. 1 to 4 in a first embodiment in schematic block rendering, see, and - FIG. 6 in another embodiment, also in schematic block rendering.
Som det vises på fig. 1 på tegningen, består det første viste ud-5 førelseseksempel for anlægget 1 i det væsentlige af følgende komponenter:As shown in FIG. 1 of the drawing, the first exemplary embodiment of the system 1 shown consists essentially of the following components:
Et arrangement af forrådsbeholdere 2, en masseblander 3, en glassmelteovn 4, en glasforarbejdningsmaskine 5, en spildgaskøler 6 og en gasrensningsindretning 7.An arrangement of storage containers 2, a mass mixer 3, a glass melting furnace 4, a glass processing machine 5, a waste gas cooler 6 and a gas cleaning device 7.
ίο Forrådsbeholderne 2 tjener til optagelse og lagring af dels af faldsforbrændingsaske 80 og dels tilsætningsstoffer 81. Ved deres ne-derste ende har forrådsbeholderne 2 hver en doseringssluse 20, fx. en cellehjulssluse. Disse doseringssluser 20 munder ind i en fælles transportindretning 21, her en snegletransportør, som munder ud i den øveris ste del af masseblanderen 3. Masseblanderen 3 har et i det væsentlige tragtformet, nedadtil indsnævret hus 30 samt en i dette hus 30 anbragt blandesnegl 31. Blandesneglen 31 forløber parallelt med indersiden af sidevæggen i huset 30 og er drejelig både om egen akse samt om en central i lodret retning gennem huset 30 i masseblanderen 3 forløbende 20 akse. I den øvre del af huset 30 er der anbragt et faststofindløb 32, som er forbundet med den førnævnte transportindretning 21. Ved den nederste ende af huset 30 i masseblanderen 3 er der anbragt et faststofudløb 33, som munder ind i en massetilførselsindretning 46. Massetilførsel sindretningen 46 danner allerede en del af glassmelteovnen 4.ίο The storage containers 2 serve for receiving and storing partly of waste incinerator box 80 and partly additives 81. At their lower end, the storage containers 2 each have a dosing sluice 20, e.g. a cell wheel lock. These metering locks 20 open into a common conveyor device 21, here a snail conveyor, which opens into the upper part of the mass mixer 3. The mass mixer 3 has a substantially funnel-shaped, downwardly narrowed housing 30 and a mixing auger 31 arranged in this housing. The mixing auger 31 extends parallel to the inside of the side wall of the housing 30 and is rotatable both about its own axis and about a center in a vertical direction through the housing 30 in the mass mixer 3 extending 20 axis. In the upper part of the housing 30 is provided a solid inlet 32 which is connected to the aforementioned conveying device 21. At the lower end of the housing 30 in the mass mixer 3 a solid outlet 33 is provided, which opens into a mass supply device 46. The mass supply the device 46 already forms part of the glass melting furnace 4.
25 Glassmelteovnen 4 består af et kar 41 af ildfast materiale, som foroven er dækket ved hjælp af en overbygning 42, ligeledes af ildfast materiale. karret 41 og overdækningen 42 hviler på en bærekonstruktion 40, som her er dannet af ståldragere. På ydersiden er overdækningen 42 af glassmelteovnen 4 omsluttet af en gastæt kappe 42', som består af stål-30 plade, og som rækker til den øverste kant af karret 41 og der er forbundet tætnende med denne. Fra oversiden er der gennem overbygningen 42 og kappen 42' indført varmeelektroder 43 gastæt i det indre af glassmelteovnen 4. Det indre af glassmelteovnen 4 er opdelt i to forskellige områder, nemlig en smeltedel, som på fig. 1 ligger til venstre, og 35 en opvarmningsdel, som på fig. 1 ligger til højre. Opdelingen af glas- - 8 - DK 169057 B1 smelteovnen 4 i de to nævnte områder sker ved hjælp af en som en del af overbygningen 42 udformet, fra denne nedragende, nedhængt, hvælvet bue 44, som under driften af glassmelteovnen 4 knapt rækker ned til oven over overfladen 84' for en i ovnen 4 tilstedeværende glassmelte 84 og 5 danner en lodret skillevæg for gasrummet i ovnen 4. Endvidere er der neden under buen 44 anbragt et parallelt med denne forløbende kølemiddelrør 45, som forløber gennem glassmelteovnen 4, og som ligger nøjagtigt i højde med overfladen 84' for glassmelten 84 og tjener til at bringe glassmelten 84 til størkning i omgivelserne af røret 45. Ved den ίο højre ende af glassmelteovnen 4 findes et glassmelteudløb 48, efter hvilket er anbragt en kun skematisk vist glasforarbejdningsmaskine 5. Ligeledes ved den højre ende af glassmelteovnen 4 er der endelig anbragt endnu en gennem overbygningen 42 opad forløbende spildgasaftræksåbning 47.The glass melting furnace 4 consists of a vessel 41 of refractory material which is covered above by a superstructure 42, also of refractory material. the tub 41 and the cover 42 rest on a support structure 40 formed here by steel carriers. On the outside, the cover 42 of the glass melting furnace 4 is enclosed by a gas-tight sheath 42 'which consists of steel 30 plate, which extends to the upper edge of the vessel 41 and is sealingly connected thereto. From the upper side, heat electrodes 43 are inserted through the superstructure 42 and the casing 42 'gas tightly into the interior of the glass melting furnace 4. The interior of the glass melting furnace 4 is divided into two different regions, namely a melting section, as in FIG. 1 is on the left, and 35 is a heating section, as in FIG. 1 is on the right. The division of the glass melting furnace 4 into the two aforementioned areas is effected by means of a part 44 of the superstructure 42 formed from this receding, suspended, arched arch 44, which during operation of the glass melting furnace 4 barely extends to above the surface 84 'of a glass melt 84 and 5 present in the furnace 4 forms a vertical partition for the gas space in the furnace 4. Further, beneath the arc 44, a parallel to this extending refrigerant pipe 45 extending through the glass melting furnace 4 is arranged. exactly at the level of the surface 84 'of the glass melt 84 and serves to solidify the glass melt 84 in the vicinity of the tube 45. At the right end of the glass melting furnace 4 is a glass melt outlet 48, after which a glass processing machine 5. is shown only schematically. Finally, at the right end of the glass melting furnace 4, another waste gas exhaust port 47 extending upwardly through the superstructure 42 is disposed.
15 Med spildgasaftræksåbningen 47 i glassmelteovnen 4 er der forbun det en varmeisoleret gasledning 60, som fører til gasindgangen 61 i spildgaskøleren 6. Foruden gasindgangen 61 har spildgaskøleren 6 en gasudgang 62 samt et udløb 63 for kondensationsprodukter, hvor gasudgangen 62 og udløbet 63 er anbragt ved den nederste ende af spildgas-20 køleren 6. Endvidere har spildgaskøleren 6 midler 65 til føring samt tilførsel og bortledning af et kølemiddel, fx. kølevand eller køleluft.15 With the waste gas extractor opening 47 in the glass melting furnace 4 there is connected a heat insulated gas line 60 which leads to the gas inlet 61 in the waste gas cooler 6. In addition to the gas inlet 61, the waste gas cooler 6 has a gas outlet 62 and an outlet 63 for condensation products, where the gas outlet 62 and the outlet 63 are arranged at the lower end of the waste gas cooler 6. Further, the waste gas cooler 6 has means 65 for guiding and supplying and discharging a refrigerant, e.g. cooling water or cooling air.
Oven over spildgaskøleren 6 er der antydet en mekanisk rensningsindretning 66, med hvilken de spildgasførende dele af spildgaskøleren 6 kan renses kontinuerligt eller periodisk for de der som følge af spildgas-25 kølingen udfældede kondensationsprodukter. Det tilhørende udløb 63 fra spildgaskøleren 6 til kondensationsprodukterne er via en yderligere transportindretning 64, her ligeledes en snegletransportør, forbundet med tilførselssiden af masseblanderen 3, dvs. den øverste del af dennes indre. Den øverste del af huset 30 i masseblanderen 3 har desuden en 30 åbning, som udgør et indløb 36 for kondensationsprodukterne. Via et udtag 69 ved den øverste ende af transportindretningen 64 kan kondensationsprodukterne efter behov udtages delvist eller helt.Above the waste gas cooler 6 there is indicated a mechanical cleaning device 66 with which the waste gas carrying parts of the waste gas cooler 6 can be cleaned continuously or periodically for the condensation products which precipitated as a result of the waste gas cooling. The associated outlet 63 from the waste gas cooler 6 to the condensation products is connected via a further conveying device 64, here also a auger conveyor, to the supply side of the mass mixer 3, ie. the upper part of its interior. In addition, the upper part of the housing 30 in the mass mixer 3 has an opening 30 which forms an inlet 36 for the condensation products. Via a receptacle 69 at the upper end of the conveying device 64, the condensation products can be partially or completely removed as needed.
Efter gasudgangen 62 på spildgaskøleren 6 er der anbragt en første sugeventilator 67, som på udgangssiden er forbundet med en forbindel-35 sesledning 68. Denne forbindelsesledning 68 fører til et gasindløb 34 - 9 - DK 169057 B1 på masseblanderen 3, hvorhos gasindløbet 34 er anbragt i den nederste del af huset 30 og er udformet således, at en indtrædning af gas til det indre af huset 30 er mulig, men en udtrædning af masse fra det indre af huset 30 til ledningen 68 er udelukket.After the gas outlet 62 on the waste gas cooler 6, a first suction fan 67 is provided, which is connected to the output side with a connecting line 68. This connecting line 68 leads to a gas inlet 34 - 9 - mass mixer 3, where the gas inlet 34 is arranged. in the lower part of the housing 30 and is designed such that an entry of gas into the interior of the housing 30 is possible, but a withdrawal of mass from the interior of the housing 30 to the conduit 68 is excluded.
5 Ved den modsat gasindløbet 34 anbragte ende, dvs. ved den øverste ende af masseblanderen 3, er der anbragt et gasudløb 35, efter hvilket en anden sugeventilator 70 er anbragt. Her er den første sugeventilator 67 og den anden sugeventilator 70 regulerbar i deres effekt, til hvilket formål de fortrinsvis er forbundet med en fælles styreindretning, ίο Fra udgangen på den anden sugeventilator 70 fører en gasledning 71 til gasrensningsindretningen 7, som kan være udformet med i og for sig kendte komponenter og derfor ikke er nærmere omtalt her. På udgangssiden er der efter gasrensningsindretningen 7 endeligt tilsluttet en skorsten 79.5 At the opposite end of the gas inlet 34, i.e. at the upper end of the mass mixer 3, a gas outlet 35 is arranged, after which another suction fan 70 is arranged. Here, the first suction fan 67 and the second suction fan 70 are adjustable in their power, for which purpose they are preferably connected to a common control device. From the output of the second suction fan 70, a gas line 71 leads to the gas cleaning device 7, which may be formed with and components known per se and are therefore not further discussed herein. On the output side, a chimney 79 is finally connected to the gas cleaning device 7.
is Det på fig. 2 viste udførelseseksempel for anlægget svarer i sine væsentligste dele til det allerede ved hjælp af fig. 1 beskrevne udførelseseksempel. Til forskel fra fig. 1 er glassmelteovnen 4 her imidlertid udført lidt anderledes. Den med det først beskrevne udførelseseksempel i glassmelteovnen 4 tilstedeværende hvælvede bue 44 er udeladt 20 ved glassmelteovnen 4 ifølge fig. 2, dvs. overdelen 42 af glassmelteovnen 4 er udformet som en gennemgående konstruktion med et enkelt ovnindre. Endvidere er kølemiddel røret 45 ved glassmelteovnen ifølge fig.ice In FIG. 2, the embodiment of the system shown in its essential parts corresponds to that already illustrated by FIG. 1. Unlike FIG. 1, however, the glass melting furnace 4 here is designed slightly differently. The vaulted arc 44 present with the first described embodiment in the glass melting furnace 4 is omitted 20 at the glass melting furnace 4 according to FIG. 2, i.e. the top 42 of the glass melting furnace 4 is designed as a continuous structure with a single furnace bottom. Further, the refrigerant tube 45 is at the glass melting furnace of FIG.
2 forskudt i retning af udløbsenden for glassmelteovnen 4, dvs. på fig.2 offset in the direction of the outlet end of the glass melting furnace 4, i. in FIG.
2 mod højre. Herved kan den på glassmelten 84 i det indre af glassmel-25 teovnen 4 svømmende masse 83 udbrede sig tilnærmelsesvis over hele overfladen af glassmelten 84 i glassmelteovnen 4. Herved opnås det, at en stor del af de fra glassmelten 84 opstigende gasser og dampe allerede kondenserer i det ovenpåliggende massedække. Spildgasmængden mindskes således. Samtidigt mindskes temperaturen af den gas, som forlader 30 glassmelteovnen 4 gennem åbningen 47. Den andrager her omkring 300 til 500°C.2 to the right. Hereby the mass 83 floating on the glass melt 84 in the interior of the glass melting furnace 4 can spread approximately over the entire surface of the glass melt 84 in the glass melting furnace 4. This results in the fact that a large part of the gases and vapors rising from the glass melt 84 in the superficial mass deck. The amount of waste gas is thus reduced. At the same time, the temperature of the gas leaving the glass melting furnace 4 is reduced through the aperture 47. It is here at about 300 to 500 ° C.
For også ved dette anlæg at sikre en sikker ødelæggelse af dioxiner og/eller furaner i den udtrædende spildgas er der i den efter gasaftræksåbningen 47 koblede gasledning 60 indsat en separat gasopvarmer 35 91. Denne gasopvarmer 91 er kun skematisk antydet på fig. 2 og kan være - 10 - DK 169057 B1 af en i og for sig kendt konstruktion. I den opvarmes den ankommende spildgas i en tid på mindst 1,5 sek til en temperatur på mindst 1200°C.In order to also ensure a safe destruction of dioxins and / or furans in the extracting waste gas at this plant, a separate gas heater 35 91. connected to the gas extraction opening 47 is installed. This gas heater 91 is only schematically indicated in FIG. 2 and may be - of a construction known per se. In it, the oncoming waste gas is heated for at least 1.5 seconds to a temperature of at least 1200 ° C.
Den yderligere konstruktion af anlægget ifølge fig. 2 svarer til konstruktionen af anlægget ifølge fig. 1, hvorhos de samme dele af an-5 læggene er betegnet med de samme henvisningsbetegnelser.The further construction of the system according to FIG. 2 corresponds to the construction of the system of FIG. 1, wherein the same parts of the systems are designated by the same reference numerals.
Det tredie udførelseseksempel for anlægget ifølge fig. 3 er især ejendommeligt ved, at spildgaskøleren 6 med den tilhørende gasledning 60 her ikke er til stede. Glassmelteovnen 4 svarer her i det væsentlige til glassmelteovnen, som er vist på fig. 2 med den forskel, at der her ίο er anbragt en gasaftræksåbning 47' ved tilførselsenden, dvs. ved den venstre ende af glassmelteovnen 4. Denne gasaftræksåbning 47' står via en kort gasledning 60' i forbindelse med sugesiden på en første sugeventilator 67. Derfra fører den allerede beskrevne forbindelsesledning 68 til masseblanderen 3.The third embodiment of the system according to FIG. 3 is particularly peculiar in that the waste gas cooler 6 with the associated gas line 60 is not present here. The glass melting furnace 4 here corresponds substantially to the glass melting furnace shown in FIG. 2 with the difference that a gas extractor opening 47 'is provided here at the supply end, i.e. at the left end of the glass melting furnace 4. This gas extractor opening 47 'communicates via a short gas line 60' with the suction side of a first suction fan 67. From there, the already described connection line 68 leads to the mass mixer 3.
is Denne masseblander 3 er, da der ikke skal tilføres kondensations- produkter fra spildgaskøleren, i sin øverste del udformet uden den ved de før beskrevne anlæg tilstedeværende tilførselsåbning 36.ice This mass mixer 3, since no condensation products from the waste gas cooler are to be supplied, is formed in its upper part without the supply opening 36 present at the plants described above.
Den til den sikre ødelæggelse af dioxiner og/eller furaner nødvendige opvarmning af spildgassen sker her ligeledes i en separat gasop-20 varmer 91, som ved anlægget ifølge fig. 3 er indkoblet i den fra den anden sugeventilator 70 til gasrensningsindretningen 7 førende spildgasledning 71.The heating of the waste gas needed for the safe destruction of dioxins and / or furans is also carried out here in a separate gas heater 91, which at the plant according to FIG. 3 is connected to the waste gas line 71 leading from the second suction fan 70 to the gas cleaning device 7.
Den sidst viste variant af anlægget ifølge fig. 4 svarer i vid udstrækning til udførelseseksemplet ifølge fig. 3, hvor forskellen her 25 ligger i, at den separate gasopvarmer 91 til opvarmningen af spildgassen og ødelæggelsen af eventuelt i denne tilstedeværende dioxiner og/ eller furaner er anbragt efter gasrensningsindretningen 7 og er indbygget i den til skorstenen 79 førende gasledning. Denne udformning af anlægget byder især på den fordel, at den til opvarmning bestemte gas-30 mængde efter gasrensningsindretningen 7 kun andrager omtrent 507« af den oprindelige gasmængde, dvs. der spares opvarmningsenergi.The last variant of the system of FIG. 4 is largely similar to the embodiment of FIG. 3, wherein the difference here 25 lies in the fact that the separate gas heater 91 for heating the waste gas and the destruction of any dioxins and / or furans present in it is arranged after the gas cleaning device 7 and is built into the gas pipe leading to the chimney 79. This design of the plant, in particular, offers the advantage that the amount of gas for heating according to the gas cleaning device 7 is only about 507 'of the original gas quantity, ie. heating energy is saved.
I det følgende skal der beskrives et proceseksempel for den fremgangsmåde, som kan gennemføres med det tidligere ved hjælp af fig. 1 beskrevne anlæg: 35 Fra et affaldsforbrændingsanlæg eller fra et depot stammende af- -11- DK 169057 B1 faldsforbrændingsaske 80 tilføres den første forrådsbeholder 2. De yderligere forrådsbeholdere 2 fyldes med nødvendige tilsætningsstoffer 81, især sand og phonolit samt eventuelt glasskår. Ved hjælp af doseringssluserne 20 udtages affaldsforbrændingsaske 80 i forudbestemte 5 mængdeforhold samt tilsætningsstofferne 81 fra forrådsbeholderne 2 og transporteres ved hjælp af transportøren 21 ind i det indre af beholderen 30 i masseblanderen 3. Der blandes de enkelte bestanddele ved hjælp af blandesneglen 31 til en homogen, til smeltning bestemt masse 82. Færdig, smeltelig masse 82 transporteres gennem faststofudløbet 33 ίο i masseblanderen 3 ved hjælp af massetilførselsindretningen 46 ind i det indre af glassmelteovnen 4. Under drift er glassmelteovnen 4 fyldt til en bestemt højde med glassmelte 84. Her ligger overfladen 84' af glassmelten 84 nøjagtigt i højde med kølemiddel røret 45 og knapt nok neden under buen 44.In the following, a process example of the process which can be carried out with the former by means of FIG. 1 described plant: 35 From a waste incineration plant or from a depot originating from -11- DK 169057 B1 waste incinerator box 80 is added to the first storage container 2. The additional storage containers 2 are filled with necessary additives 81, especially sand and phonolite as well as any glass shards. By means of the metering locks 20, waste incinerator box 80 is taken in predetermined 5 proportions and the additives 81 from the storage containers 2 and transported by means of the conveyor 21 into the interior of the container 30 in the mass mixer 3. The individual components are mixed by means of the mixing screw 31 into a homogeneous. for melting determined mass 82. Finished, meltable mass 82 is conveyed through solid outlet 33 or into mass mixer 3 by means of mass feed device 46 into the interior of the glass melting furnace 4. In operation, the glass melting furnace 4 is filled to a certain height with glass melt 84. Here lies the surface 84 'of the glass melt 84 exactly at the height of the refrigerant tube 45 and barely below the arc 44.
is Den af massetilførselsindretningen 46 tilførte masse svømmer som smeltende masse 83 på glassmelten 84 og fordeler sig på dennes overflade 84' i smeltedelen, dvs. på fig. 1 den venstre del, af glassmelteovnen 4. Da glassmelten 84 omkring kølemiddel røret 45 bringes til at stivne ved hjælp af det gennemstrømmende kølemiddel, kan den smeltende 20 masse 83 ikke komme over i den del af glassmelteovnen, som befinder sig på den anden side af buen 44 og kølemiddel røret 45. Den til smeltningen af massen 83 nødvendige varmeenergi frembringes her ved hjælp af varme-elektroderne 43, som med deres nederste del rager ned i glassmelten 84, som joulesk energi i glassmelten 84, hvorhos glassmelten 84 danner den 25 ohmske modstand.ice The mass supplied by the mass supply device 46 swims as melting mass 83 on the glass melt 84 and distributes on its surface 84 'in the melting portion, ie. in FIG. 1 in the left part of the glass melting furnace 4. As the glass melt 84 around the coolant tube 45 is caused to solidify by the flowing refrigerant, the melting mass 83 cannot enter the part of the glass melting furnace which is on the other side of the arc 44 and coolant tube 45. The heat energy needed for the melting of the mass 83 is here produced by the heat electrodes 43, which project with their lower part into the glass melt 84, as joules of energy in the glass melt 84, whereby the glass melt 84 forms the 25 ohmic resistance.
Under smeltningen af massen 83 stiger spildgasser 85 op fra denne, hvor spildgassen her har en temperatur mellem ca. 100 og 1000°C og i det væsentlige kan indeholde S08, HC1, chlorider, sulfater, kuldioxid, alkali- og tungmetaldampe samt dioxiner og/eller furaner.During the melting of the mass 83, waste gases 85 rise from the latter, where the waste gas here has a temperature between approx. 100 and 1000 ° C and may contain substantially SO8, HCl, chlorides, sulfates, carbon dioxide, alkali and heavy metal fumes as well as dioxins and / or furans.
30 Denne spildgas 85 træder gennem spalten mellem undersiden af over karmen 44 og kølemiddel røret 45 ind i den højre del af det indre af glassmelteovnen 4. I denne del af glassmelteovnen 4 er overfladen 84' af glassmelten 84 fri for massen. Den i denne del af glassmelteovnen 4 tilstedeværende glassmelte 84 har en temperatur på ca. 1400°C. Tempera-35 turen i den øverste del af glassmelteovnen 4 oven over smelten 84 an- - 12 - DK 169057 B1 drager her i det mindste omtrent 1300 - 1350°C. For her at opnå en højst mulig temperatur er overdelen 42 af glassmelteovnen 4 hensigtsmæssigt stærkt varmeisoleret. Den i dette område af glassmelteovnen 4 indtrædende spildgas efteropvarmes nu ved varmeoptagelse fra smelten, 5 hvor der ved indstilling af strømningshastigheden og ved valg af passende dimensioner af glassmelteovnen 4 kan drages omsorg for, at temperaturen af den varme spildgas 86 i det mindste i en periode på 1,5 sek. opnår en størrelse på mindst 1200°C. Herved ødelægges de eventuelt i den ankommende spildgas 85 indeholdte dioxiner og/eller furaner med ίο sikkerhed, således at den varme spildgas 86 kun indeholder chlorider, sulfater, kuldioxiden samt alkali- og tungmetaldampene.This waste gas 85 enters through the gap between the underside of the frame 44 and the coolant tube 45 into the right part of the interior of the glass melting furnace 4. In this part of the glass melting furnace 4, the surface 84 'of the glass melt 84 is free of the pulp. The glass melt 84 present in this part of the glass melting furnace 4 has a temperature of approx. 1400 ° C. The temperature in the upper part of the glass melting furnace 4 above the melt 84 is here at least about 1300 - 1350 ° C. In order to achieve the highest possible temperature, the top 42 of the glass melting furnace 4 is suitably highly insulated. The waste gas entering this area of the glass melting furnace 4 is now reheated by heat absorption from the melt 5, whereby by adjusting the flow rate and by selecting the appropriate dimensions of the glass melting furnace 4, the temperature of the hot waste gas 86 can be at least for a period of time. in 1.5 sec. attains a size of at least 1200 ° C. In this way, the dioxins and / or furans contained in the arriving waste gas 85 may be destroyed with certainty, so that the hot waste gas 86 contains only chlorides, sulphates, the carbon dioxide as well as the alkali and heavy metal vapors.
Denne varme spildgas 86 trækkes ud gennem den varmeisolerede ledning 60, hvorhos dennes varmeisolering i det væsentlige tjener til at forhindre en afkøling og dermed kondensation af den varme spildgas 86 is inden i ledningen 60. Den varme spildgas 86 kommer gennem gasindgangen 61 ind i spildgaskøleren 6, hvor den afkøles til en temperatur mellem 300 og 500°C. Derved kondenserer en del af spildgassen og slår sig ned inden i spildgaskøleren 6. De fremkommende kondensationsprodukter 88 fjernes periodisk eller kontinuerligt ved hjælp af renseindretningen 66 20 og føres til det neden under spildgaskøleren 6 anbragte udløb 63 til kondensationsproduktet. Derfra føres kondensationsprodukterne 88 ved hjælp af transportindretningen 64 gennem indløbet 36 til kondensationsprodukterne ind i det indre af masseblanderen 3 og føres således tilbage til den til smeltning bestemte masse 82. Efter behov kan kondensa-25 ti onsprodukterne 88 sluses helt eller delvist gennem udtaget 69.This hot waste gas 86 is drawn out through the heat insulated conduit 60, its heat insulation essentially serving to prevent a cooling and thus condensation of the hot waste gas 86 ice within the conduit 60. The hot waste gas 86 enters through the gas inlet 61 into the waste gas cooler 6 where it is cooled to a temperature between 300 and 500 ° C. Thereby, a portion of the waste gas condenses and settles within the waste gas cooler 6. The resulting condensation products 88 are removed periodically or continuously by the cleaning device 66 20 and fed to the outlet 63 located below the waste gas cooler 6 to the condensation product. From there, the condensation products 88 are passed through the inlet 36 through the inlet 36 to the condensation products into the interior of the mass mixer 3 and thus are returned to the mass 82 for melting. As required, the condensation products 88 can be completely or partially closed through the outlet 69.
Den gennem gasudgangen 62 fra spildgaskøleren udtrædende, forafkølede spildgas 87 kommer ind i den første sugeventilator 67. Denne sørger for, at der på dens sugeside, dvs. inden i spildgaskøleren 6, i ledningen 60 samt i det indre af glassmelteovnen 4 hersker et undertryk 30 i forhold til omgiveIseslufttrykket. På transportsiden sørger sugeventilatoren 67 for, at den fra denne udtrædende, forafkølede spildgas 87 inden i forbindelsesledningen 68 til en masseblander 3 får et overtryk i forhold til omgivelseslufttrykket. Denne under et overtryk stående, forafkølede spildgas 87 ledes gennem gasindløbet 34 ind i den til 35 smeltning bestemte masse 82 i det indre af masseblanderen 3. Under gen- - 13 - DK 169057 B1 nemstrømningen af spildgassen 87 køles denne under yderligere kondensation til en temperatur på mellem 20 og 50°C og træder ved overfladen af den til smeltning bestemte masse 82 ud som kold spildgas. Blandesneglen 31 sørger desuden for en gennemblånding af de enkelte bestanddele af 5 den til smeltning bestemte masse 82 således, at sidstnævnte forbliver luftig og gasgennemtrængelig. På grund af den stærke afkøling kondenserer der inden i den til smeltning bestemte masse 82 også dampe ved lave temperaturer, som fx. tungmetal dampe. Den gennem gasudløbet 35 fra masseblanderen 3 udtrædende kolde spildgas 89 indeholder da i det væ-io sentlige kun HC1 og S02.The pre-cooled waste gas 87 exiting through the gas outlet 62 from the waste gas cooler enters the first suction fan 67. This ensures that on its suction side, ie. inside the waste gas cooler 6, in the conduit 60 and in the interior of the glass melting furnace 4, a negative pressure 30 prevails in relation to the ambient air pressure. On the transport side, the suction fan 67 ensures that the exiting, pre-cooled waste gas 87 within the connection conduit 68 to a mass mixer 3 receives an overpressure relative to the ambient air pressure. This pressurized pre-cooled waste gas 87 is passed through the gas inlet 34 into the mass 82 for the melting of the interior of the mass mixer 3. During the flow of the waste gas 87, it is cooled to a temperature under further condensation. of between 20 and 50 ° C and exits at the surface of the melt 82 determined as cold waste gas. In addition, the mixing auger 31 provides a mixing of the individual components of the mass 82 for melting, so that the latter remains airy and gas permeable. Due to the strong cooling, within the mass 82 for melting, vapors also condense at low temperatures, such as e.g. heavy metal fumes. The cold waste gas 89 coming out of the gas outlet 35 from the mass mixer 3 then contains essentially only HCl and SO2.
Den efter gasudløbet 35 efterkoblede anden sugeventilator 70 sørger her i forbindelse med en passende styreenhed samt tryksensorer for, at trykket af den kolde spildgas 89 i den øvre del af masseblanderen 30 i det væsentlige forbliver lig med omgivelseslufttrykket. Dette bidra-15 ger til, at hverken spildgas kan komme ud i omgivelserne eller falsk luft ind i systemet.The second suction fan 70 coupled to the gas outlet 35 here in connection with a suitable control unit as well as pressure sensors here ensures that the pressure of the cold waste gas 89 in the upper part of the mass mixer 30 remains substantially equal to the ambient air pressure. This contributes to the fact that neither waste gas can enter the environment nor false air into the system.
Den kolde spildgas 89, i det væsentlige en koncentreret gas af chlorider og S02 samt S03, føres via ledningen 71 til gasrensningsindretningen 7 og renses dér yderligere. De fra gasrensningsindretningen 20 udtrædende, endnu resterende restspildgasser 90, især N2, C02 og små mængder ilt frigøres endeligt gennem skorstenen 79 til omgivelserne.The cold waste gas 89, essentially a concentrated gas of chlorides and SO2 as well as SO3, is fed via line 71 to the gas purifier 7 and further purified there. The residual residual waste gases 90 emerging from the gas purification device 20, in particular N 2, CO 2 and small amounts of oxygen, are finally released through the chimney 79 to the surroundings.
Her er en risiko eller beskadigelse af miljøet som følge af de relativt harmløse bestanddele, som danner restspi Idgassen 90, udelukket.Here, a risk or damage to the environment due to the relatively harmless constituents that form residue Idgassen 90 are excluded.
Ud over restspildgassen 90 leverer anlægget 1 ifølge det viste ud-25 førelseseksempel efter den beskrevne fremgangsmåde glaslegemer 9 som genanvendeligt råstof, der ved hjælp af glasforarbejdningsmaskinen 5 fremstilles af den udløbende glassmelte 84" ved kontinuerlig produktion. Disse glaslegemer 9 kan fx. anvendes som skærver eller betontilslag.In addition to the residual waste gas 90, the plant 1 according to the illustrated embodiment provides, according to the described process, glass bodies 9 as recyclable raw material which is produced by the glass processing machine 5, which is produced by the continuous glass melt 84 "by continuous production. or concrete aggregate.
30 Størrelsen af glassmelteovnen 4 og dermed volumenet af den i den tilstedeværende glassmelte 84 vælges hensigtsmæssigt så stor, at forekommende svingninger i sammensætningen af affaldsforbrændingsasken ikke fuldstændigt kan ændre det smeltede glas kortvarigt i dets kemi. Opstående ændringer i sammensætningen af glassmelten 84 kan meget hurtigt, 35 fx. ved hjælp af ændringerne i den elektriske modstand af glassmelten - 14 - DK 169057 B1 84 mellem elektroderne 43, opdages. Disse måleværdier kan da anvendes til regulering af blandingen af affaldsforbrændingsasken 80 og de enkelte tilskudsstoffer 81, især et tilskudsstof med et vist al kali indhold, fx. phonolit.The size of the glass melting furnace 4, and thus the volume of the glass melt 84 present, is suitably chosen so large that fluctuations in the composition of the waste incinerator box cannot completely change the molten glass in its chemistry for a short time. Emerging changes in the composition of the glass melt 84 can very quickly, 35 e.g. by means of the changes in the electrical resistance of the glass melt between the electrodes 43 are detected. These measurement values can then be used to regulate the mixture of the waste incinerator box 80 and the individual additives 81, in particular a supplement with a certain potassium content, e.g. phonolite.
5 En yderligere mulighed for korrektion af sammensætningen af glas smelten 84 består i, at krystallisationsforekomster iagttages ved det færdige glasprodukt. Specifikke glassammensætninger i grænseområdet danner bestemte krystaller, som let kan opdages i det færdige glas, og som angiver, om og til hvilken side sammensætningen af glasset har for-lo andret sig. Tilsvarende kan mængderne af den til blanding bestemte affaldsforbrændingsaske 80 og tilskudsstofferne 81 varieres.A further possibility of correcting the composition of the glass melt 84 is to observe crystallization occurrences at the finished glass product. Specific glass compositions in the boundary region form particular crystals which are readily detectable in the finished glass and indicate whether and to which side the composition of the glass has changed. Similarly, the amounts of the waste incinerator box 80 to be blended and the additive 81 can be varied.
Ved hjælp af fig. 5 og 6 skal to udførelseseksempler for gasrensningsindretningen 7 forklares i det følgende, hvorhos fig. 5 viser en våd-gasrensningsindretning 7 og fig. 6 en tør- henholdsvis halvtør-gas-15 rensningsindretning 7.By means of FIG. 5 and 6, two exemplary embodiments of the gas cleaning device 7 will be explained in the following, wherein FIG. 5 shows a wet gas cleaning device 7 and FIG. 6 is a dry and semi-dry gas cleaning device 7 respectively.
Ifølge fig. 5 kommer den kolde spildgas 89 gennem ledningen 71 ind i et første vaskertrin 72. I dette første vaskertrin udvaskes især HC1 fra spildgassen. I et andet vaskertrin 72' udvaskes derpå især S02. I en efterfølgende dråbeudskiller 73 udskilles medrevne vanddråber. I en 20 gas-opvarmningsstrækning 74 varmes gassen til en egnet temperatur mellem 30 og 90°C og føres derpå til et aktivt kul-filtertrin 78. Efter disses gennemløb kommer restspildgassen 90, i det væsentlige sammensat af N2, C02 og små mængder ilt gennem skorstenen 79 ud i omgivelserne.According to FIG. 5, the cold waste gas 89 enters through a conduit 71 into a first washing step 72. In this first washing step, HC1 in particular is washed out of the waste gas. Then, in another washing step 72 ', SO 2 is washed out in particular. In a subsequent droplet separator 73, entrained water droplets are separated. In a gas gas heating section 74, the gas is heated to a suitable temperature between 30 and 90 ° C and then passed to an active carbon filter stage 78. After their passage, the residual waste gas 90, composed essentially of N 2, CO 2 and small amounts of oxygen, passes through chimney 79 into the surroundings.
I det første vaskertrin 72 til HC1-udskillelsen skal der indstil-25 les en pH-værdi i det sure område, fortrinsvis mindre end 1. Det andet vaskertrin 72' til S02-udskillelsen fungerer derimod fortrinsvis basisk med ρΗ-værdier på fx. 6 - 7,5. Begge vaskertrinene 72 og 72' fungerer fortrinsvis i modstrøm, men kan imidlertid også fungere i medstrøm. Eventuelt tilstedeværende kviksølvmængde i spildgassen 89 udskilles 30 fuldstændigt i det aktive kul-filtertrin 78. De fra vaskertrinene 72 og 72' samt fra dråbeudskilleren 73 afgivne udstødsmængder til spildevand og slam føres hensigtsmæssigt til et spildevandsrensningsanlæg.In the first washing step 72 for the HCl secretion, a pH value must be set in the acidic region, preferably less than 1. The second washing step 72 'for the SO2 separation, on the other hand, preferably works basically with ρΗ values of e.g. 6 - 7.5. Both washing steps 72 and 72 'preferably operate in countercurrent, but can also operate in co-current. Any amount of mercury present in the waste gas 89 is 30 completely separated in the active carbon filter stage 78. The effluents and sludge exhaust quantities emitted from the washing stages 72 and 72 'and from the droplet separator 73 are suitably fed to a wastewater treatment plant.
Det andet udførelseseksempel for gasrensningsindretningen 7 ifølge fig. 2b har som en første komponent en befugter 75, til hvilken der lige-35 ledes gennem ledningen 71 føres den kolde spildgas 89. Efter mætning af - 15 - DK 169057 B1 spilgassen i befugteren 75 føres den til en hvirvellags- eller sprøjte-adsorber 76. Sprøjteadsorberen påvirkes fortrinsvis med NaOH eller Ca(OH)2 i vandig opløsning. Den udtrædende gas bringes i et gas-tempereringstrin 77 op på den for det her følgende aktive kul-filtertrin 78 5 optimale temperatur. Den til sidst udtrædende restspi Idgas 90 kommer også her atter gennem skorstenen 79 ud til omgivelserne.The second embodiment of gas cleaning device 7 according to FIG. 2b, as a first component, has a humidifier 75 to which is directly passed through the conduit 71, the cold waste gas 89 is passed. After saturation of the waste gas in the humidifier 75, it is fed to a vortex or spray adsorber 76 The spray adsorber is preferably treated with NaOH or Ca (OH) 2 in aqueous solution. The leaving gas is brought up in a gas tempering step 77 to the optimum temperature for the following active carbon filter stage 78. The finally leaving residue Idgas 90 also comes here again through chimney 79 to the surroundings.
Det her udskilte spildevand samt de her udfældede faststoffer føres ligeledes til en yderligere rensningsindretning, fx. et spildevandsrensningsanlæg, eller deponering eller genanvendelse, ίο På grund af den relativt enkle, veldefinerede sammensætning af spildgassen 89 kan gasrensningsindretningerne 7 tjene til genindvinding af natriumchlorid og natriumsulfat i relativt ren form. Disse råstoffer kan atter anvendes til fremstillingen af fx. soda.The effluent here separated and the precipitated solids are also fed to a further purification device, e.g. a wastewater treatment plant, or landfill or recycling, ο Because of the relatively simple, well-defined composition of the waste gas 89, the gas cleaning devices 7 can serve to recover sodium chloride and sodium sulfate in relatively pure form. These raw materials can again be used for the production of e.g. soda.
Som allerede beskrevet føres den i relativt små mængder udfældede is spildgas enten direkte eller efter gennemledningen gennem massen til støvudskillelse i en støvudskiller og renses derpå i en vådrensning. I et yderligere trin føres spildgassen derpå gennem et aktivt kulfilter, hvorhos den derpå opstående rengas uden videre kan udledes til atmosfæren, da den ikke mere indeholder miljøbelastende partikler eller gas-20 mængder.As already described, in relatively small amounts of precipitated ice wastewater is passed either directly or after the passage through the pulp to a dust separator in a dust separator and then purified in a wet cleaning. In a further step, the waste gas is then passed through an activated carbon filter, whereupon the resulting gas can be discharged to the atmosphere without further delay, since it no longer contains environmentally harmful particles or gas volumes.
Det er overraskende for fagmanden, at en væsentlig formindskelse af miljøbelastningen ifølge opfindelsen kan opnås ved, at både det udskilte støv og filtratet fra vådindretningen eller slammet fra gasrensningen atter kan tilføres massen af tilskudsstoffer og affaldsforbræn-25 dings-filteraske og efter en blanding med massen atter kan føres ind i glassmelteovnen.It is surprising to those skilled in the art that a significant reduction of the environmental impact of the invention can be achieved by the addition of both the separated dust and the filtrate from the wet device or the sludge from the gas purification to the mass of additives and waste combustion filter ash and after mixing with the mass. can again be introduced into the glass melting furnace.
Fremgangsmåden ifølge opfindelsen har flere fordele. For det første udtages kun to materialer fra processen. Først materialet for glasset, der kan finde anvendelse ved vejbygning eller i lignende anvendel-30 sestilfælde, og dernæst glasgallen, som er sammensat af alle saltene, hvis opløselighedsgrænse i glassmelten ved glassmelteprocessen og graden af det indsmeltede glas overskrides.The method of the invention has several advantages. First, only two materials are removed from the process. First, the material for the glass that can be used in road construction or similar applications, and then the glass bile, which is composed of all the salts whose solubility limit in the glass melt during the glass melt process and the degree of the molten glass is exceeded.
De totale mængder af de af processen udvundne skadestoffer mindskes herved med de i gasrensningen udfældede stoffer og de deri inde-35 holdte tungmetaller. Da opløselighedsgrænsen for metallerne og i videre - 16 - DK 169057 B1 forstand for alle tungmetaller i glassmelten ikke nås ved processen, bindes samtlige tungmetaller udvaskningssikkert i glasset ved tilbageføringen.The total quantities of the pollutants obtained by the process are thereby reduced by the substances precipitated in the gas purification and the heavy metals contained therein. Since the solubility limit for the metals and in the further sense of all heavy metals in the glass melt is not reached by the process, all heavy metals are bonded to the glass in a safe leach during the return.
Det er endvidere overraskende for fagmanden, at resten af giasgal-5 le er relativt ren, da en eksakt udskillelse er mulig som følge af den i forhold til den foreslåede fremgangsmåde større gallemængde, og gallen dermed når en større renhedsgrad. Der opstår således mulighed for at afsætte denne glasgalle som råstof til den kemiske industri. Mængden af glasgallen andrager ca. mellem 5-10% af den indgivne affaldsforbræn-10 dingsaskemængde.Furthermore, it is surprising to those skilled in the art that the remainder of the bile bile is relatively pure, since an exact separation is possible as a result of the larger bile quantity relative to the proposed process and the bile thus reaches a higher degree of purity. Thus, it is possible to market this glass bile as a raw material for the chemical industry. The amount of the glass bile is approx. between 5-10% of the submitted waste incineration box quantity.
Claims (32)
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE3830899 | 1988-09-10 | ||
DE3830899 | 1988-09-10 | ||
DE3841889 | 1988-12-13 | ||
DE3841889A DE3841889A1 (en) | 1988-09-10 | 1988-12-13 | Process for converting solid, substantially anhydrous waste materials into the glass form (vitrification) and apparatus for carrying out the process |
DE19893904613 DE3904613A1 (en) | 1989-02-16 | 1989-02-16 | Environmentally friendly process for converting solid waste materials into glass form (vitrification) |
DE3904613 | 1989-02-16 |
Publications (3)
Publication Number | Publication Date |
---|---|
DK441489D0 DK441489D0 (en) | 1989-09-07 |
DK441489A DK441489A (en) | 1990-03-11 |
DK169057B1 true DK169057B1 (en) | 1994-08-08 |
Family
ID=27198209
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DK441489A DK169057B1 (en) | 1988-09-10 | 1989-09-07 | Process for the transfer of solid, almost anhydrous glass waste and plants for carrying out the process |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP0359003B1 (en) |
JP (1) | JPH07102977B2 (en) |
AU (1) | AU624414B2 (en) |
DE (1) | DE58906363D1 (en) |
DK (1) | DK169057B1 (en) |
ES (1) | ES2047074T3 (en) |
Families Citing this family (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4977837A (en) * | 1990-02-27 | 1990-12-18 | National Recovery Technologies, Inc. | Process and apparatus for reducing heavy metal toxicity in fly ash from solid waste incineration |
CH680198A5 (en) * | 1990-07-06 | 1992-07-15 | Sulzer Ag | |
DE4035777A1 (en) * | 1990-11-08 | 1992-05-14 | Noell Gmbh | METHOD FOR THE DISPOSAL OF DUST CONTAINING TOXIC HEAVY METALS, TOXIC ORGANIC MATERIALS AND SIMILAR COMPOUNDS |
DE4111385A1 (en) * | 1991-04-09 | 1992-10-15 | Leybold Ag | Filter dust smelting with reduced electrode erosion - in which electrodes are inserted into glass from above into mixt. of dust and additives |
DE4112162C1 (en) * | 1991-04-13 | 1992-07-30 | Beteiligungen Sorg Gmbh & Co Kg, 8770 Lohr, De | |
WO1993001141A1 (en) * | 1991-07-11 | 1993-01-21 | Schoenhausen Horst | Process and device for the safe disposal of toxic residues |
SK277897B6 (en) * | 1991-09-23 | 1995-07-11 | Pavel Vlcek | Vitrification method of powdered waste, mainly light ash from flue ash |
FR2684573B1 (en) * | 1991-12-05 | 1994-10-07 | Mediterranee Const Ind | PROCESS FOR THE TREATMENT OF SOLID RESIDUES FROM THE PURIFICATION OF FUMES FROM AN INCINERATION FURNACE TO PERFORM FOR THEM, FOR VITRIFICATION OR MELTING, AND ITS INSTALLATION. |
DE4301353C1 (en) * | 1993-01-20 | 1994-05-26 | Sorg Gmbh & Co Kg | Method of vitrifying waste material contg. high proportion of carbon - with heat generated by burning gases used to heat up material fed to appts. |
FR2719793A1 (en) * | 1993-07-30 | 1995-11-17 | Cnim | Vitrification of solid residues for incineration |
FR2708490B1 (en) * | 1993-07-30 | 1995-11-10 | Cnim | Vitrification process for solid residues from the incineration of household and / or industrial waste, device for the implementation of this process and product from this process. |
FR2711077B1 (en) * | 1993-10-11 | 1996-01-05 | Delot Int Fours | Waste vitrification process, and vitrification furnace. |
DE4424950C2 (en) * | 1994-07-14 | 1997-02-13 | Flachglas Ag | Device for withdrawing gaseous products and for draining the glass melt and their use |
FR2726492B1 (en) * | 1994-11-09 | 1997-01-17 | Electricite De France | ADJUVANT AND PROCESS FOR THE STABILIZATION OF WASTE CONTAINING METAL ELEMENTS |
KR0158083B1 (en) * | 1995-06-07 | 1998-12-15 | 신재인 | Vitrification method of high radioactive waste material using flyash |
FR2746037B1 (en) * | 1996-03-13 | 1998-05-15 | PROCESS FOR THE VITRIFICATION TREATMENT OF ASBESTOSED WASTE, PARTICULARLY FROM THE BUILDING, AND INSTALLATION FOR CARRYING OUT SAID METHOD | |
JPH11201439A (en) * | 1998-01-12 | 1999-07-30 | Ishikawajima Harima Heavy Ind Co Ltd | Ash-melting furnace |
KR100360215B1 (en) * | 1998-09-11 | 2002-11-08 | 닛폰 고칸 가부시키가이샤 | Method for melting incineration residue containing salts and apparatus therefor |
FR2816529B1 (en) * | 2000-11-13 | 2003-09-05 | Rech S De Traitement Des Deche | PROCESS FOR TREATING INCINERATION RESIDUES AND INSTALLATION FOR CARRYING OUT SUCH A PROCESS |
CZ20033117A3 (en) * | 2001-05-16 | 2004-09-15 | Owens Corning | Glass melting furnace and operation method thereof |
FR2870758B1 (en) * | 2004-05-26 | 2006-08-04 | Commissariat Energie Atomique | METHOD FOR COMBUSTION AND COMPLETE OXIDATION OF THE MINERAL FRACTION OF A TREATED WASTE IN A DIRECT COMBUSTION-VITRIFICATION APPARATUS |
CN107089795B (en) * | 2017-03-29 | 2021-09-14 | 天津壹鸣环境科技股份有限公司 | Method for melting treatment and resource utilization of household garbage incineration fly ash electrode |
DE102018108418A1 (en) * | 2018-04-10 | 2019-10-10 | Schott Ag | Process for the preparation of glass products and apparatus suitable for this purpose |
CN113289441A (en) * | 2021-06-04 | 2021-08-24 | 中国矿业大学 | Device and method for purifying domestic garbage cracking gasification tail gas |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2631220C2 (en) * | 1976-07-12 | 1986-03-06 | Sorg-GmbH & Co KG, 8770 Lohr | Melting furnace for melting radioactive substances in glass |
GB8331031D0 (en) * | 1983-11-21 | 1983-12-29 | Roberts D | Vitrification of asbestos waste |
US4652289A (en) * | 1984-11-26 | 1987-03-24 | Hydro-Quebec | Purification of effluent gases |
US4632690A (en) * | 1985-06-04 | 1986-12-30 | Colwell Jr Robert E | Hazardous waste removal method and apparatus |
US4666490A (en) * | 1986-02-12 | 1987-05-19 | Drake Ronald N | Aqueous waste vitrification process and apparatus |
DE3631729A1 (en) * | 1986-09-18 | 1988-03-24 | Gea Luftkuehler Happel Gmbh | Process for the catalytic conversion of nitrogen oxides in the flue gases arising in glass manufacture |
-
1989
- 1989-08-25 EP EP89115675A patent/EP0359003B1/en not_active Expired - Lifetime
- 1989-08-25 ES ES89115675T patent/ES2047074T3/en not_active Expired - Lifetime
- 1989-08-25 DE DE89115675T patent/DE58906363D1/en not_active Expired - Fee Related
- 1989-09-04 AU AU41060/89A patent/AU624414B2/en not_active Ceased
- 1989-09-07 DK DK441489A patent/DK169057B1/en not_active IP Right Cessation
- 1989-09-11 JP JP1235478A patent/JPH07102977B2/en not_active Expired - Lifetime
Also Published As
Publication number | Publication date |
---|---|
EP0359003A2 (en) | 1990-03-21 |
JPH07102977B2 (en) | 1995-11-08 |
AU4106089A (en) | 1990-03-15 |
DE58906363D1 (en) | 1994-01-20 |
EP0359003A3 (en) | 1991-01-16 |
EP0359003B1 (en) | 1993-12-08 |
DK441489A (en) | 1990-03-11 |
JPH02175620A (en) | 1990-07-06 |
ES2047074T3 (en) | 1994-02-16 |
AU624414B2 (en) | 1992-06-11 |
DK441489D0 (en) | 1989-09-07 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DK169057B1 (en) | Process for the transfer of solid, almost anhydrous glass waste and plants for carrying out the process | |
US4944785A (en) | Process using melt accelerator for the conversion of solid waste substances into glass | |
US6319482B1 (en) | Treatment of fly ASH/APC residues including lead salt recovery | |
US4666490A (en) | Aqueous waste vitrification process and apparatus | |
US5027722A (en) | Process and device for processing slag and other combustion residues from waste incineration plants | |
CN110201975A (en) | A kind of abraum salt recycling treatment disposal system and application | |
ES2438536T3 (en) | Procedure for reprocessing bypass powders and products that can be obtained from it | |
CN108870405A (en) | A kind of hazardous waste collection disposing technique | |
HU210639B (en) | Procedure for operating of glass-melting furnace | |
SE450041B (en) | SET AND DEVICE FOR CONVERTING WASTE FROM A HAZARDOUS TO A RELATIVELY HAZARDOUS CONDITION | |
SE438787B (en) | PROCEDURE FOR CLEANING OF EXHAUST GAS FROM INDUSTRIES AND SLUER DISPOSAL FOR IMPLEMENTATION OF THE PROCEDURE | |
EP2734283A1 (en) | Method for removing impurities from flue gas condensate | |
CN207238730U (en) | Reclaimer is burned in a kind of negative-pressure cyclic accumulation of heat that harmlessness disposing is carried out to high saliferous chemical engineering sludge | |
US5032161A (en) | Apparatus for melting asbestos-containing waste material in glass | |
US5093103A (en) | Process for separating off poisonous volatile chemical compounds from a mixture of solid particles having a particle size of up to 200 microns | |
KR101951139B1 (en) | TRE TYPE WASTE NaS BATTERY DISASSEMBLING SYSTEM | |
US6315810B1 (en) | Process for vitrifying heavy-metal-containing residues having a chlorine content above 10% by mass and a melting furnace for carrying out the process | |
BRPI0604307B1 (en) | electrohydrometallurgical process in alkaline medium for zinc extraction of electric furnace powder | |
FR2642327A1 (en) | IMPROVEMENTS IN SMOKE PURIFICATION PROCESSES | |
JPH0587288B2 (en) | ||
CN112139200A (en) | Incineration fly ash disposal process and system thereof | |
CA1334792C (en) | Process for converting solid, dehydrated waste substances into glass | |
NO783643L (en) | WASTE TREATMENT PROCEDURES | |
JP2003002611A (en) | Treating method for filtrate from ash washing | |
CN115228885A (en) | Method for treating fly ash generated by waste incineration |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
B1 | Patent granted (law 1993) | ||
PBP | Patent lapsed |