NO151124B - PROCEDURE FOR THE RECOVERY OF MAGNESIUM BISULPHITE - Google Patents
PROCEDURE FOR THE RECOVERY OF MAGNESIUM BISULPHITE Download PDFInfo
- Publication number
- NO151124B NO151124B NO781789A NO781789A NO151124B NO 151124 B NO151124 B NO 151124B NO 781789 A NO781789 A NO 781789A NO 781789 A NO781789 A NO 781789A NO 151124 B NO151124 B NO 151124B
- Authority
- NO
- Norway
- Prior art keywords
- magnesium
- accordance
- monosulphite
- sulfur dioxide
- bisulphite
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims description 37
- LPHFLPKXBKBHRW-UHFFFAOYSA-L magnesium;hydrogen sulfite Chemical compound [Mg+2].OS([O-])=O.OS([O-])=O LPHFLPKXBKBHRW-UHFFFAOYSA-L 0.000 title claims description 14
- 238000011084 recovery Methods 0.000 title claims description 10
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 55
- JESHZQPNPCJVNG-UHFFFAOYSA-L magnesium;sulfite Chemical compound [Mg+2].[O-]S([O-])=O JESHZQPNPCJVNG-UHFFFAOYSA-L 0.000 claims description 28
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 16
- 239000011593 sulfur Substances 0.000 claims description 14
- 229910052717 sulfur Inorganic materials 0.000 claims description 14
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 13
- 239000000395 magnesium oxide Substances 0.000 claims description 12
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 12
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 claims description 10
- 238000010521 absorption reaction Methods 0.000 claims description 10
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 238000003776 cleavage reaction Methods 0.000 claims description 6
- 230000007017 scission Effects 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- 239000011777 magnesium Substances 0.000 claims description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 4
- 239000003518 caustics Substances 0.000 claims description 4
- 229910052749 magnesium Inorganic materials 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 239000005864 Sulphur Substances 0.000 claims description 2
- 239000000654 additive Substances 0.000 claims description 2
- 238000004090 dissolution Methods 0.000 claims description 2
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims 1
- 229910021653 sulphate ion Inorganic materials 0.000 claims 1
- 239000002253 acid Substances 0.000 description 15
- 239000000126 substance Substances 0.000 description 6
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 5
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 4
- 230000002378 acidificating effect Effects 0.000 description 3
- 239000001913 cellulose Substances 0.000 description 3
- 229920002678 cellulose Polymers 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000004992 fission Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- APVPOHHVBBYQAV-UHFFFAOYSA-N n-(4-aminophenyl)sulfonyloctadecanamide Chemical compound CCCCCCCCCCCCCCCCCC(=O)NS(=O)(=O)C1=CC=C(N)C=C1 APVPOHHVBBYQAV-UHFFFAOYSA-N 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/42—Magnesium sulfites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/48—Sulfur dioxide; Sulfurous acid
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C11/00—Regeneration of pulp liquors or effluent waste waters
- D21C11/06—Treatment of pulp gases; Recovery of the heat content of the gases; Treatment of gases arising from various sources in pulp and paper mills; Regeneration of gaseous SO2, e.g. arising from liquors containing sulfur compounds
- D21C11/063—Treatment of gas streams comprising solid matter, e.g. the ashes resulting from the combustion of black liquor
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Geology (AREA)
- Biomedical Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Description
Den foreliggende oppfinnelse vedrører en fremgangsmåte til gjenvinning av magnesiumbisulfitt fra avgasser fra en lutfor-brenningskjei, hvor absorpsjon av svoveldioksyd foregår i minst ett magnesiummonosulfittrinn og minst ett magnesiumbisulfittrinn. The present invention relates to a method for recovering magnesium bisulphite from exhaust gases from a caustic incineration boiler, where absorption of sulfur dioxide takes place in at least one magnesium monosulphite stage and at least one magnesium bisulphite stage.
Kjente fremgangsmåter til fremstilling av cellulose på magnesiumbasis inndeles kjemisk i to grupper: Known methods for the production of magnesium-based cellulose are divided chemically into two groups:
a) Magnefitt-metode a) Magnefitt method
Fra DE-off.skrift 1.933.647 er det kjent å fremstille svovel-forbindelser av avgasser fra kraftverk eller cellulosefabrikker, hvorved S02 først bindes til Mg og deretter frigjøres igjen ved varmeinnvirkning. Derved dannes det en gass med høyt SC^-innhold, From DE-off.skrift 1,933,647 it is known to produce sulfur compounds from exhaust gases from power plants or cellulose factories, whereby S02 is first bound to Mg and then released again by heat. This creates a gas with a high SC^ content,
som er råstoffkilde for svovelforbindelsene som skal fremstilles. which is the raw material source for the sulfur compounds to be produced.
Det fremgår ikke fra off.skriftet hvordan det kan fremstilles magnesiumbisulfitt på en slik måte at det i et mellomtrinn dannes mer magnesiumsulfitt enn det som er nødvendig for bisulfittfremstillingen. Overskuddet av sulfitt spaltes. Fremgangsmåten ifølge off.skriftet er således ikke egnet for en lukket syklisk prosess hvor SC^-innholdet i overskuddsproduktene er regulerbart og kan ledes bort gjennom et avløp. It is not clear from the official document how magnesium bisulphite can be produced in such a way that more magnesium sulphite is formed in an intermediate step than is necessary for the production of bisulphite. The excess sulphite is decomposed. The method according to the publication is thus not suitable for a closed cyclic process where the SC^ content in the excess products is adjustable and can be led away through a drain.
Betrakter man totalkjemikaliene ser man at kjemikalieomløpet, som tilsvarer innholdet i tårnsyren, ved magnefittmetoden gjennom-snittlig er større enn ved den sure metode, slik at på basis av den sure metode (=100%) er det for MgO ca. 100% og for S ca. 40% høyere. If you consider the total chemicals, you can see that the chemical cycle, which corresponds to the content of the tower acid, with the magnetite method is on average greater than with the acidic method, so that on the basis of the acidic method (=100%) it is for MgO approx. 100% and for S approx. 40% higher.
Dersom man ifølge begge fremgangsmåter vil oppnå samme råstofforbruk ved samme cellulosekvalitet, så betyr dette at tapsandelen ifølge magnefittmetoden må være mindre i samme grad som det økte kjemikalieomløp. Dette betyr en fordel for den sure metode. F.eks. gjelder følgende: for MgO: En gjenvinningsgrad ved den sure metode på 90% krever en gjenvinningsgrad ved magnefittmetoden på 95%, for S: En gjenvinningsgrad ved den sure metode på 90% krever en gjenvinningsgrad ved magnefittmetoden på 93%. If, according to both methods, the same raw material consumption will be achieved with the same cellulose quality, this means that the proportion of losses according to the magnetite method must be smaller to the same extent as the increased chemical circulation. This means an advantage for the acidic method. E.g. the following applies: for MgO: A recovery rate by the acid method of 90% requires a recovery rate by the magnetite method of 95%, for S: A recovery rate by the acid method of 90% requires a rate of recovery by the magnetite method of 93%.
De kjente magnesiumbisulfittmetoder med kjemikaliegjen-vinning kan av svovelet, som utelukkende gjenvinnes via trykk-luten, i beste fall frembringe nesten ren, støkiometrisk bisulfittsyre, imidlertid ikke syre med oppløst svovel i form av S02. The known magnesium bisulphite methods with chemical recovery can at best produce almost pure, stoichiometric bisulphite acid from the sulphur, which is exclusively recovered via the pressure lye, but not acid with dissolved sulfur in the form of SO2.
Ifølge de kjente metoder kan det frembringes råsyrer hvori følgende prosentandeler svovel mangler, regnet av det støkio-metrisk bundete bisulfittiske svovel i tårnsyren: Magnefitt: ca. 4-5%, ved den sure metode: ca. 3-4%. According to the known methods, raw acids can be produced in which the following percentages of sulfur are missing, calculated from the stoichiometrically bound bisulphite sulfur in the tower acid: Magnefitt: approx. 4-5%, by the acid method: approx. 3-4%.
Omdannelsen av den 100 prosentige bisulfittsyre respektivt av det frie svovel i bisulfittsyren til tårnsyre foregår i det såkalte konsentrasjonstårn ved hjelp av S02~konsentratgass med minst 15 volumprosent S02 fra et svovelforbrenningsanlegg. Dette anlegg tilføres den svovelmengde som tilsvarer de totale tap i systemet. Denne konsentrering kan også utføres med flytende S02-Disse prosessteknisk betingete syredannelsesnødvendigheter bevirker at ifølge begge metoder er det nødvendig med minimum-svoveltap for fremstilling av den nødvendige syre. Disse material-tap er: for magnefitt: 3,5 - 4,5% av totalsvovelmengden i tårnsyren, og for den sure metode: 23 - 3 0% av totalsvovelmengden i tårnsyren (ved 100% virkningsgrad ved konsentreringen). The conversion of the 100 percent bisulfite acid, respectively of the free sulfur in the bisulfite acid to tower acid takes place in the so-called concentration tower with the help of S02~concentrate gas with at least 15 volume percent S02 from a sulfur combustion plant. This facility is supplied with the amount of sulfur corresponding to the total losses in the system. This concentration can also be carried out with liquid SO2 - These process-related acid formation requirements mean that, according to both methods, a minimum sulfur loss is required for the production of the required acid. These material losses are: for magnefit: 3.5 - 4.5% of the total amount of sulfur in the tower acid, and for the acid method: 23 - 30% of the total amount of sulfur in the tower acid (at 100% efficiency during the concentration).
Ifølge bestående og ventede bestemmelser er disse belast-ninger på miljøet utelatelige, spesielt for den sure metode, særlig idet 30% av disse tap forlater anlegget som gassformig so2. According to existing and expected regulations, these burdens on the environment are negligible, especially for the acid method, particularly as 30% of these losses leave the plant as gaseous SO2.
Formålet med den foreliggende oppfinnelse er å tilføre til kokeriet ved fullstendig lukket kjemikaliekretsløp en kokesyre hvis andel av fysikalsk løst S02 kan velges.fritt. The purpose of the present invention is to add a cooking acid whose proportion of physically dissolved SO 2 can be chosen freely to the cooker in a completely closed chemical circuit.
Fremgangsmåten ifølge oppfinnelsen kjennetegnes'ved at det ved absorpsjonen frembringes mer magnesiummonosulfitt enn det som er nødvendig for bisulfittfremstillingen, og at overskuddsmengden, som tilsvarer differansen mellom svovelmengden i tykkluten og det totale, sulfatisk og sulfittisk bundete svovel i tårnsyren, føres ut av magnesiumbisulfittomløpet i form av magnesiummonosulfitt. Særlig anvendes det uttatte magnesiummonosulfitt som råstoff for svovelsyrefremstilling. Fortrinnsvis spaltes det uttatte magnesiummonosulfitt under innvirkning av varme i svoveldioksyd og magnesiumoksyd, og det frembrakte svoveldioksyd løses i den rensete bisulfittløsning, mens magnesiumoksydet f.eks. til-bakeføres til monosulfittrinnet. Med fordel spaltes det uttatte magnesiummonosulfitt utelukkende ved termisk spalting uten tilsetningsstoffer i temperaturområdet mellom 500 og 900°C, hvorved fortrinnsvis spaltingen av magnesiummonosulfittet foregår ved hjelp av en del av den varme som frigjøres i lutforbrenningskjelen. Ifølge et ytterligere trekk ved oppfinnelsen spaltes magnesiummonosulfitten i magnesiumoksyd og svoveldioksyd, og svoveldioksydet kondenseres. Særlig tørkes magnesiumonosulfitten før spaltingen, og spaltingen av magnesiummonosulfitten foregår ved indirekte oppvarming, fortrinnsvis i en gasstrøm, som hovedsakelig består av svoveldioksyd. Ifølge et ytterligere trekk ved oppfinnelsen bringes en delstrøm av det frembrakte svoveldioksyd i berøring med magnesiumbisulfittløsningen, som er dannet i et absorpsjonstrinn i en venturiformet fallkanal i finblæret form, hvorved det foregår en oppløsning av svoveldioksydet. Fortrinnsvis bringes svoveldioksydet inn i det minste tverrsnitt av den venturiformete fallkanal gjennom fine kanaler, fortrinnsvis fine boringer. The method according to the invention is characterized by the fact that more magnesium monosulphite is produced during the absorption than is necessary for bisulphite production, and that the excess amount, which corresponds to the difference between the amount of sulfur in the thick liquor and the total sulphitic and sulphitic bound sulfur in the tower acid, is carried out of the magnesium bisulphite circuit in the form of magnesium monosulphite. In particular, the withdrawn magnesium monosulphite is used as a raw material for sulfuric acid production. Preferably, the extracted magnesium monosulphite is decomposed under the influence of heat into sulfur dioxide and magnesium oxide, and the produced sulfur dioxide is dissolved in the purified bisulphite solution, while the magnesium oxide e.g. is fed back to the monosulphite step. Advantageously, the extracted magnesium monosulphite is decomposed exclusively by thermal decomposition without additives in the temperature range between 500 and 900°C, whereby the decomposition of the magnesium monosulphite preferably takes place with the help of part of the heat released in the lye combustion boiler. According to a further feature of the invention, the magnesium monosulphite is split into magnesium oxide and sulfur dioxide, and the sulfur dioxide is condensed. In particular, the magnesium monosulphite is dried before the cleavage, and the cleavage of the magnesium monosulphite takes place by indirect heating, preferably in a gas stream, which mainly consists of sulfur dioxide. According to a further feature of the invention, a partial flow of the produced sulfur dioxide is brought into contact with the magnesium bisulphite solution, which is formed in an absorption step in a venturi-shaped drop channel in fine-vested form, whereby a dissolution of the sulfur dioxide takes place. Preferably, the sulfur dioxide is brought into the smallest cross-section of the venturi-shaped drop channel through fine channels, preferably fine bores.
Oppfinnelsen vil bli nærmere forklart i det etterfølgende under henvisning til de medfølgende tegninger, hvori: Fig. 1 viser prosesskjerna for et monosulfittspaltings-anlegg. Fig. 2 viser et termisk koplingsskjema for et liknende anlegg. The invention will be explained in more detail below with reference to the accompanying drawings, in which: Fig. 1 shows the process core for a monosulphite splitting plant. Fig. 2 shows a thermal connection diagram for a similar plant.
I fig. 1 transporteres en vandig magnesiumsulfittsuspensjon fra et magnesiumbisulfittgjenvinningsanlegg til en sentrifuge 1 og konsentreres til et tørrstoffinnhold på over 70% og transporteres via en snekke 2 til en strømtørker 3. Vannet som fraskilles i sentrifugen 1 strømmer gjennom en ledning 13 tilbake i magnesiumbisulfittgjenvinningsanlegget. Det tørkete, krystal-linske magnesiummonosulfitt fraskilles i en sentrifugalkraft-separator 4, som er innkoplet etter strømtørkeren 3, og faller ned i en samlebeholder 5. Luften fra tørkeren innføres i magnesiumbisulf ittanlegget av sentrifugalseparatoren. Magnesiummonosulfitten tilføres via en møllehjulsluse 6 og en transportsnekke 7 til et termisk sulfittspaltingsanlegg 8, som blir drevet i et temperaturområde på fortrinnsvis 500 - 900°C. Ved disse tem-peraturer s<p>altes magnesiummonosulfitt i magnesiumoksyd og svoveldioksyd. Svoveldioksydet trykkes via en vifte 9 innad i en gasskjøler 10 hvor det avkjøles til ca. 65°C og føres inn i konsentreringstårnet for dannelse av fritt, oppløst svovel i form av SO^ i magnesiumbisulfittløsningen. Svoveldioksydet kan imidlertid også kondenseres. Magnesiumoksydet forlater spaltingsanlegget 8 via en falltrakt og en møllehjulsluke 11 In fig. 1, an aqueous magnesium sulphite suspension is transported from a magnesium bisulphite recovery plant to a centrifuge 1 and concentrated to a dry matter content of over 70% and transported via a screw 2 to a flow dryer 3. The water separated in the centrifuge 1 flows through a line 13 back into the magnesium bisulphite recovery plant. The dried, crystalline magnesium monosulphite is separated in a centrifugal force separator 4, which is connected after the flow dryer 3, and falls into a collection container 5. The air from the dryer is introduced into the magnesium bisulphite plant by the centrifugal separator. The magnesium monosulphite is supplied via a mill wheel sluice 6 and a transport screw 7 to a thermal sulphite splitting plant 8, which is operated in a temperature range of preferably 500 - 900°C. At these temperatures, magnesium monosulphite dissolves into magnesium oxide and sulfur dioxide. The sulfur dioxide is pressed via a fan 9 into a gas cooler 10 where it is cooled to approx. 65°C and fed into the concentration tower to form free, dissolved sulfur in the form of SO^ in the magnesium bisulphite solution. However, the sulfur dioxide can also be condensed. The magnesium oxide leaves the splitting plant 8 via a drop funnel and a mill wheel hatch 11
og innføres i en hydratiseringsbeholder 12 hvor det oppslemmes i vann og pumpes i form av oppløst magnesiumhydroksyd inn i magnesiumbisulfittgjenvinningsanlegget som absorbens for svoveldioksydet . and introduced into a hydration container 12 where it is slurried in water and pumped in the form of dissolved magnesium hydroxide into the magnesium bisulphite recovery plant as an absorbent for the sulfur dioxide.
I fig. 2 er den termiske spalting i spaltingsreaktoren 8 vist nærmere. Spaltingsreaktoren oppvarmes indirekte ved hjelp av brennkammeret 14 ved hjelp av oppvarmingsgass som er oppvarmet til ca. 900°C. Oppvarmingsgassen som strømmer ut av spaltingsreaktoren 8 og som er avkjølt til ca. 800°C avkjøles i en varmeutveksler 15 til ca. 600°C og innføres i en tørker 16 for magnesiummonosulf itten. Gassen forlater denne tørker ved ca. 400°C In fig. 2, the thermal cleavage in the cleavage reactor 8 is shown in more detail. The fission reactor is heated indirectly by means of the combustion chamber 14 by means of heating gas that is heated to approx. 900°C. The heating gas which flows out of the fission reactor 8 and which has cooled to approx. 800°C is cooled in a heat exchanger 15 to approx. 600°C and introduced into a dryer 16 for the magnesium monosulphite. The gas leaves this dryer at approx. 400°C
og tilføres til slutt en ytterligere varmeutveksler 17 hvor den and is finally supplied to a further heat exchanger 17 where it
o o
avkjøles til ca. 300 C, som omtrent er lik avgasstemperaturen for en lutforbrenningskjel 26, og innføres i kjelens røkgass-ledning 18 foran et absorpsjonsanlegg 27. cool to approx. 300 C, which is roughly equal to the exhaust gas temperature for a caustic incineration boiler 26, and is introduced into the boiler's flue gas line 18 in front of an absorption system 27.
Fra absorpsjonsanlegget 27 uttas en delstrøm av den frem-stilte, fuktige magnesiummonosulfitt og tilføres til tørkeren 16. Den tørkete magnesiumsulfitt bringes via en sluse 19 inn i sulfittspaltingsanlegget 8 hvor det opprettholdes en spaltings-temperatur på 800°C. Sulfittspaltingsanlegget 8 gjennomstrømmes av en varm, svoveldioksydholdig gassblanding, som når den strøm-mer ut inneholder vanndamp og MgO-støv, og som etter utstrømmingen fra sulfittspaltingsanlegget avkjøles til ca. 200°C i en regene-reringsvarmeutveksler 20, i en varmeutvekslersyklon 21 samt i en varmeutveksler 23, før den ved hjelp av en vifte 22 delvis gjennom en kondensator 25 tilføres til en konsentreringsanordning 24. I varméutvekslersyklonen 21 fraskilles MgO-støvet, som er dannet ved spaltingen, og tilføres igjen til absorpsjon sa n 1 e cj g et 27. Etter viften 22 tilbakeføres den overveiende del.,ay .SO.^-gass- .. blandin<g>en via varmeutvekslerne 20 og 15 igjen til ...sulf it.tspal;t-.; ..-, ingsanlegget som bærergass, hvorved de i varmeutvekslerne 20 og . 15 oppvarmes igjen nesten til spaltingstemperaturen. A partial flow of the produced moist magnesium monosulphite is taken from the absorption plant 27 and supplied to the dryer 16. The dried magnesium sulphite is brought via a sluice 19 into the sulphite splitting plant 8 where a splitting temperature of 800°C is maintained. The sulphite splitting plant 8 is flowed through by a hot, sulfur dioxide-containing gas mixture, which when it flows out contains water vapor and MgO dust, and which, after the outflow from the sulphite splitting plant, is cooled to approx. 200°C in a regeneration heat exchanger 20, in a heat exchanger cyclone 21 and in a heat exchanger 23, before it is supplied by means of a fan 22, partly through a condenser 25, to a concentrating device 24. In the heat exchanger cyclone 21, the MgO dust, which is formed, is separated during the splitting, and is supplied again to absorption sa n 1 e cj g et 27. After the fan 22, the predominant part. .sulf it.tspal;t-.; ..-, ing plant as carrier gas, whereby the in the heat exchangers 20 and . 15 is heated again almost to the cleavage temperature.
For bedre varmeutnyttelse forvarmes brennstoffet og/el ler f orbrenningsluf ten i henholdsvis varmeutvekslersyklo.nen 21. og varmeutveksleren 17. Konsentreringsanordningen 24 består. hoved.-: sakelig av et venturirør som er anordnet i en lukket beholder.,. og svoveldioksydet innføres i rørets trangeste parti og løses opp i råsyren som føres i kretsløp. ,. For better heat utilization, the fuel and/or combustion air is preheated in the heat exchanger cyclone 21 and the heat exchanger 17, respectively. The concentrating device 24 consists. main.-: matter of a venturi tube which is arranged in a closed container.,. and the sulfur dioxide is introduced into the narrowest part of the pipe and dissolved in the crude acid which is circulated. ,.
Ifølge oppfinnelsen er det mulig å foreta oppvarmingen, av spaltingsanlegget direkte eller indirekte i røkgasstrømmen fra lutforbrenningskjelen 26. Dessuten er det mulig, når det er........ nødvendig med senket behov for syre i bisulfittløsningen, å According to the invention, it is possible to carry out the heating of the splitting plant directly or indirectly in the flue gas flow from the caustic incineration boiler 26. Furthermore, it is possible, when it is... necessary with a reduced need for acid in the bisulphite solution, to
ta ut en del av den i absorpsjonsanlegget frembrakte._MgS.Qg fra kjemikaliekretsløpet og f.eks. viderearbeide den til svovelsyre. take out a part of the one produced in the absorption plant._MgS.Qg from the chemical cycle and e.g. further process it into sulfuric acid.
Claims (11)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AT404177A AT347236B (en) | 1977-06-08 | 1977-06-08 | PROCESS FOR THE RECOVERY OF MAGNESIUM BISULPHITE FROM THE AGBASEN OF A LYE INCINERATOR |
Publications (3)
Publication Number | Publication Date |
---|---|
NO781789L NO781789L (en) | 1978-12-11 |
NO151124B true NO151124B (en) | 1984-11-05 |
NO151124C NO151124C (en) | 1985-02-13 |
Family
ID=3558848
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
NO781789A NO151124C (en) | 1977-06-08 | 1978-05-23 | PROCEDURE FOR THE RECOVERY OF MAGNESIUM BISULPHITE |
Country Status (8)
Country | Link |
---|---|
AT (1) | AT347236B (en) |
CS (1) | CS237301B2 (en) |
DE (1) | DE2823749C3 (en) |
FI (1) | FI67414C (en) |
NO (1) | NO151124C (en) |
PL (1) | PL110895B1 (en) |
SE (1) | SE447736B (en) |
YU (1) | YU42480B (en) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AT383163B (en) | 1985-06-27 | 1987-05-25 | Chemiefaser Lenzing Ag | METHOD FOR REGENERATING DIGESTIVE SOLUTION FROM THE USED COOKING LUG OF A MAGNESIUM BISULFITE DIGESTIVE METHOD, AND FILTER APPARATUS FOR IMPLEMENTING THE METHOD |
AT396694B (en) * | 1992-02-14 | 1993-11-25 | Waagner Biro Ag | METHOD FOR GENERATING A HOMOGENEOUS EXHAUST GAS |
AT397929B (en) * | 1992-12-04 | 1994-08-25 | Chemiefaser Lenzing Ag | METHOD AND SYSTEM FOR DRYING AND SUBJECT CLEAVING |
-
1977
- 1977-06-08 AT AT404177A patent/AT347236B/en not_active IP Right Cessation
-
1978
- 1978-05-23 NO NO781789A patent/NO151124C/en unknown
- 1978-05-31 SE SE7806363A patent/SE447736B/en not_active IP Right Cessation
- 1978-05-31 DE DE2823749A patent/DE2823749C3/en not_active Expired
- 1978-06-06 FI FI781791A patent/FI67414C/en not_active IP Right Cessation
- 1978-06-07 YU YU1364/78A patent/YU42480B/en unknown
- 1978-06-07 PL PL1978207432A patent/PL110895B1/en unknown
- 1978-06-08 CS CS783755A patent/CS237301B2/en unknown
Also Published As
Publication number | Publication date |
---|---|
PL207432A1 (en) | 1979-04-23 |
DE2823749B2 (en) | 1979-04-12 |
AT347236B (en) | 1978-12-11 |
DE2823749A1 (en) | 1978-12-21 |
YU136478A (en) | 1983-01-21 |
NO781789L (en) | 1978-12-11 |
YU42480B (en) | 1988-10-31 |
CS237301B2 (en) | 1985-07-16 |
SE447736B (en) | 1986-12-08 |
NO151124C (en) | 1985-02-13 |
PL110895B1 (en) | 1980-08-30 |
DE2823749C3 (en) | 1981-06-19 |
FI67414C (en) | 1985-03-11 |
FI781791A (en) | 1978-12-09 |
ATA404177A (en) | 1978-04-15 |
FI67414B (en) | 1984-11-30 |
SE7806363L (en) | 1978-12-09 |
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