SE191081C1

SE191081C1 -

Info

Publication number: SE191081C1
Authority: SE
Publication date: 1964-01-01

Description

Uppfinnare: F Schytil Prioritet begard from den 18 ma) och 29 juni 1951 (Forbundsrepubliken Tyskland) Det är kant att reducera zinkoxidhaltigt ramaterial med kol under inledning av hilt i virvlande skikt, varvid virvelskiktet befinner sig i ett reaktionsrum, vars oppningsvinkel tilltar uppat. Utvidgningen av reaktionsrummets tvargenomskarning dimensioneras darvid sá, att den genom de uppstaende reaktionerna ZnO C = Zn CO CO2 C = 2C0 betingade volymsokningen just utjamnas, sa att gashastigheten blir konstant over apparatens niva. Inventor: F Schytil Priority requested from 18 May) and 29 June 1951 (Federal Republic of Germany) It is possible to reduce zinc oxide-containing raw material with carbon during the introduction of hilt in a swirling layer, the vortex layer being in a reaction chamber, the opening angle of which increases upwards. The expansion of the transverse intersection of the reaction space is dimensioned in such a way that the volume increase due to the resulting reactions ZnO C = Zn CO CO2 C = 2CO is just equalized, so that the gas velocity becomes constant above the level of the apparatus.

Det är aven kant att halla kornig gasmassa eller kalk svavande i en uppat sig utvidgande konisk behallare, i vilken fran spetsen inledes en hiirarstriim uppat av sä hog hastighet, att godset icke kan falla ned. Efter avslutning av processen, alltsfa sedan gasmassan forbrukats, eller sedan kalken reagerat med klorgas till klorkalk, installes gastillforseln och det fasta materiaet faller ned och kan uttagas efter oppnandet av en sluss. Vidare ãr det kant att i relativt smala koniska behallare nedifran inleda sã mycket gas, att det inforda fasta materialet medryckes och kan fOras uppat. Dylika anordningar ha sarskilt f8reslagits till torkning. Harvid har det i sjalva verket lyckats, att bygga I praktiken realiserbara apparater om konens oppning gjordes mycket srnal. Apparaterna arbeta som normala pneumatiska transportsystem, varvid endast stigroret uppvisar en diffusorartad utvidgning. Man anvander harvid aven samma oppningsvinkel som vid normala diffusorer eller venturiror, vilka endast beskickas med gas eller vatska. Denna oppningsvinkel a uppgar som bekant till 8°. It is also advisable to keep granular gas mass or lime floating in an upwardly expanding conical container, in which from the tip a hair strip is started upwards at such a high speed that the goods cannot fall down. At the end of the process, at least after the gas mass has been consumed, or after the lime has reacted with chlorine gas to chlorine lime, the gas supply is installed and the solid material falls down and can be taken out after opening a lock. Furthermore, it is advisable to introduce so much gas into relatively narrow conical containers from below that the introduced solid material is entrained and can be carried upwards. Such devices have been specifically suggested for drying. In fact, it has succeeded in building devices that could be realized in practice if the opening of the cone was made very special. The devices operate as normal pneumatic transport systems, with only the riser showing a diffuser-like expansion. The same opening angle is also used as with normal diffusers or venturi, which are only charged with gas or liquid. This opening angle a is, as is well known, 8 °.

Apparater enligt ovan omnarnnda forslag, i vilka det fasta godset skall virvla stationart, ha hittills icke kunnat tbyggas i tekniskt anvandbara dimensioner. Apparatus according to the above-mentioned proposals, in which the solid goods are to swirl stationary, have hitherto not been possible to build in technically usable dimensions.

Det ãr vidare kant att bromsa ett kornigt fast material, som man later falla genom ett vertikalt ror, medelst en uppatriktad gasstrom, och att man vid mycket omsorgfull installning av gashastigheten av det extra tillskottet av hastighet hos det fasta materialet tillfalligt kan styra detta i form av en fritt svavande zon, varvid hela tiden partiklar falla nedat. I tranga ror liknar detta tilltappningsforloppet vid pneumatisk transport. Om emellertid rOrdiametern gores stOrre an 10 cm, krymper existensomradet for detta igensattningsforlopp ihop, sá att det blir praktiskt taget omojligt att uppratthalla det langre tid och vid den minsta storning (andring av gashastigheten och/eller formen, storleken och/ eller specifika vikten hos de fasta partiklarna och/eller deras mangd) varken drives god-set upp eller faller ohindrat nedat. It is further edge to brake a grainy solid material, which is allowed to fall through a vertical rudder, by means of an upwardly directed gas stream, and that with very careful installation of the gas velocity the extra addition of velocity of the solid material can be temporarily controlled in the form of a free-floating zone, with particles constantly falling downwards. In narrow pipes, this is similar to the tapping process in pneumatic transport. However, if the pipe diameter is made larger than 10 cm, the area of existence of this clogging process shrinks, so that it becomes practically impossible to maintain it for a long time and at the smallest size (change in gas velocity and / or shape, size and / or specific gravity of the the solid particles and / or their quantity) are neither driven up-goods nor fall down unhindered.

Det har nu befunnits att broms- och igensattningsforloppet i ett uppatriktat, uppat oppet venturiror har ett mycket storre stabilitetsomrade. Apparater i de allra storsta dimensioner kunna salunda byggas for manga hundra tons produktion per dag. Gashastigheten installes harvid, sa att i den nedre delen sa stora friktionskrafter utovas pa de suspen- 2— — derade partiklarna, att icke alla partiklar, utan endast en del av dessa falla ned. Darefter bildas en stabil stoppzon, som svanger av och an och over vilken en fritt svavande virvlande suspension uppbygges. It has now been found that the braking and clogging process in an upright, upturned venturi has a much larger stability area. Apparatus in the largest dimensions can thus be built for many hundreds of tons of production per day. The gas velocity is then installed so that in the lower part such large frictional forces are exerted on the suspended particles that not all particles, but only a part of them fall down. Then a stable stop zone is formed, which oscillates from time to time and over which a free-floating swirling suspension is built up.

Detta forlopp far ej fi5rvaxlas med fOrloppet i trattformade virvelskiktsreaktorer, vid vilka forhallandet mellan diametern vid spetsen och vid ovre delen av behallaren ungefar Overstiger vardet 1: 20. Om en dylik behallare fylles med kornigt fast material, sa kunde detta under tyngdkraftens inverkan endast strOmma langsamt ut och vid inledning av gas fordelar sig denna i form av blasor inuti god-set och ett tatt stationiirt virvelskikt uppstar. This process must not be confused with the process in funnel-shaped fluidized bed reactors, in which the ratio between the diameter at the tip and at the upper part of the tank approximately exceeds the value of 1:20. out and at the inlet of gas it is distributed in the form of bubbles inside the goods-set and a taken stationary vortex layer arises.

Det liar vidare befunnits att stabilitetsomradet for uppdnpningsforloppet okas utomordentligt, om man later veriturirorets Oppningsvinkel tillta uppat, sa att gashastigheten avtar hastigare uppat, an som motsvarat tvarsnittets hojdokning. Detta kan ske kontinuerligt eller i olika steg. I den undre delen kan till och med vdljas en st5rre oppningsvinkel an som är tillittligt och vanligt for endast med gas eller vatska beskickade diffusorer. Man kan alltsâ valja a stone an 8°. En maximal vinkel av 0 i ovre delen skall emellertid icke overskridas. En sa framstalld reaktor kan byggas i mycket stora dimensioner och erbjuder aven fordelar, da stationara suspensioner, som salunda icke falla nedat, uppdammas och uppvirvlas. En ytterligare fordel med denna atgard, ligger dari, att den m edger anbringandet av vasentligt mera virvelgods i ett reaktionsrum av bestamd Mid an i en apparat med konstant oppningsvinkel. Under det att i en smal diffusor med konstant Oppningsvinkel virvelgodset praktiskt taget genomgar apparaten endast en gang, fores det harvid av gasstrommen Hera ganger nedat och ater upp- varigenom partikelkoncentrationen alias och en langre uppehallstid erhalles. Denna extra genomvirvling kan enligt en utveckling av uppfinningen forbattras ytterligare darigenom att den nedifran tillfOrda barargasen icke tillfores centralt utan i sidled, sa att den anbringas ojamt till gasintradesmunstycket. Darvid bildas forutom den normala virvel- rOrelsen :liven en apparaten vasentligen vertikalt genomga.ende, ungefar cirkel- till spiralformad virvel, som astadkommer en ytterligare grundlig blandning av reaktionsgodset. It has further been found that the stability range of the opening process increases excellently, if the opening angle of the vertebral tube is allowed to increase upwards, so that the gas velocity decreases more rapidly upwards than that corresponding to the height increase of the cross section. This can be done continuously or in different steps. In the lower part, even a larger opening angle can be chosen, which is reliable and common for diffusers loaded only with gas or liquid. You can therefore choose a stone at 8 °. However, a maximum angle of 0 in the upper part shall not be exceeded. Such a reactor can be built in very large dimensions and also offers advantages, as stationary suspensions, which thus do not fall down, are dusted and swirled. A further advantage of this operation lies in the fact that it allows the application of substantially more vortex in a reaction chamber of a certain Mid in an apparatus with a constant opening angle. While in a narrow diffuser with a constant opening angle the vortex practically passes through the apparatus only once, it is then fed by the gas stream Hera times downwards and again whereby the particle concentration alias and a longer residence time are obtained. According to a development of the invention, this additional vortex can be further improved by the fact that the bar gas supplied from below is not supplied centrally but laterally, so that it is applied unevenly to the gas inlet nozzle. In this case, in addition to the normal vortex motion, the device forms a substantially vertically continuous, approximately circular to helical vortex, which provides a further thorough mixing of the reaction material.

Pa atfoljande ritning forklaras sattet enligt uppfinningen ytterligare i samband med fig. 1. In the following drawing, the method according to the invention is further explained in connection with Fig. 1.

Vid A inmatas virvelgodset kontinuerligt i den ovre delen. Genom lamplig installning av gashastigheten intrader uppdamning, varvid I undre delen en stoppzon av hogre partikelkoncentration utbildas, fran vilken hela tiden partiklar skjuta uppat. Den uppburna mang- den blir konstant och det inforda Overskottet regnar hela tiden ned. Vid. B är gashastigheten okad i forhallande till A och ingenting faller langre ned. Han far man emellertid icke lang- re fora in nagot, emedan apparaten annnars skulle bli for full och fyllningen skulle som eAl propp i form av en kompakt massa drivas upp och titer storta nedat. Vid C installes gashastigheten pa ett sd stort varde, att materia- let drives ivag uppat. Genom fordelningen av punkterna i figuren antydes cirkulationen inuti suspensionen. I figurens nedre del visas ett diagram, vilket visar tryckftirlusternas forhallande till gashastigheten for en suspension i konen enligt uppfinningen. Trycket, som bararstrommen maste overvinna, heron pa godsmangden, som befinner sig 1 apparaten. Om apparaten dr torn, installes den med L (tomgang) betecknade tryckfOrlust-hastighetslinjen. Harvid stiger, som ar att vanta, med okande gashastighet trycket forst liniart och sedan ungefar kvadratiskt. At A, the vortex is fed continuously into the upper part. By suitable installation of the gas velocity, evaporation enters, whereby in the lower part a stop zone of higher particle concentration is formed, from which particles constantly shoot upwards. The amount carried becomes constant and the imported surplus is constantly raining down. At. B, the gas velocity is increased in relation to A and nothing falls further down. However, it is no longer allowed to insert anything, because otherwise the apparatus would become too full and the filling would, like a plug in the form of a compact mass, be pushed up and titer large downwards. At C, the gas velocity is installed at such a large value that the material is driven upwards. The distribution of the points in the figure indicates the circulation inside the suspension. In the lower part of the figure a diagram is shown, which shows the relation of the pressure fluctuations to the gas velocity of a suspension in the cone according to the invention. The pressure which the carrier drum must overcome, in addition to the quantity of goods present in the apparatus. If the appliance pulls the tower, install the pressure loss speed line denoted by L (idle). In this case, as is to be expected, with increasing gas velocity, the pressure rises first linearly and then approximately square.

Om man nu vid liten gashastighet tillfOr virvelgods, faller detta forst ohindrat igenom. Vid en viss granshastighet uppdammes en del, som med okande gashastighet forst endast i liten grad okas. Tryckforlusten blir darigenom hogre an vid tomgangskurvan och man en-hailer i detta stabila uppdamningsomrade en linje, som endast lutar nagot mera an torn- ngskurvan. Okar man gashastigheten over ett visst varde, Madras nedfallandet mer och mer och trycket stiger brant, apparaten blir overbeskickad och man kommer mycket fort till ett instabilt °radicle. Om virvelgodsets inforingshastighet Ras, 'inner man en hogre tryckforlust och tryckforlust-hastighetskurvorna lopa parallellt. If you now supply vortex goods at a low gas velocity, this first falls through unhindered. At a certain spruce speed, a part is dusted, which with increasing gas speed only increases to a small degree. The pressure loss is thus higher than at the idle curve and a line is hailed in this stable dam area, which only slopes slightly more than the tower curve. If you increase the gas velocity above a certain value, Madras falls more and more and the pressure rises steeply, the device becomes overloaded and you get to an unstable ° radicle very quickly. If the feed rate of the vortex is Ras, a higher pressure loss is entered and the pressure loss velocity curves run in parallel.

Vid hogre gashastigheter faller som redan namnts icke nagonting ned langre och man befinner sig omradet B far den stationara virvelsuspensionen. Ju mer virvelgods som pa en gang infores i apparaten, desto hogre blir den motsvarande tryckfOrlusten, men desto mindre blir aven variationsiajligheten for gashastigheten. Vid maximalbelastning befinner man sig pa toppen av det medelst den punktstreckade linj en begransade existensomradet, och vid den minsta storning blir forloppet instabilt. De kanda fOrslagen att i motsvarighet till maximet arbeta med mycket finkornigt gods, dvs. halla det finkorniga godset hell och hallet svavande, aro icke realiserbara i praktiken, emedan vid finkornigt gods existensomradet krymper ihop, sá att de tilllatna granserna for gashastigheten under praktisk drift oundvikligen maste Over- resp. underskridas. Arbetar man daremot med grovt material, dvs. med partikelstorlekar av flera mm storlek, kan detta omrade praktiskt realiseras, varvid hastigheten hos barargasen i munstycket, alltsa i apparatens nedersta del uppgaende till ungefar 40 m/sek, ungefar motsvarar maximalbelastningen, alltsâ toppen av den punktstreckade kurvan. Vid annu hogre gashastigheter och vid anvandning av finkornigt material, dvs. dylikt med partikelstorlekar av ungefar 1 mm, kommer man in i om- — —3 radet C for den pneumatiska transporten. Aven har aro tryckforlusterna hogre an i tom-gang och for olika matarhastigheter erhalles parallella tryckforlustkurvor. Om gashastigheten är for liten bortfores materialet ej och man kommer, som antydes med den punkterade bOrjan av tryekfOrlustkurvorna, in i ett instabilt omra'de. At higher gas velocities, as already mentioned, nothing falls down any longer and you are in area B before the stationary vortex suspension. The more vortex that is introduced into the appliance at once, the higher the corresponding pressure loss, but the smaller the variability of the gas velocity. At maximum load, one is at the top of the limited area of existence by means of the dotted line, and at the smallest disturbance the course becomes unstable. They know the proposals to work with very fine-grained goods, ie. keep the fine-grained goods well and the hall floating, are not feasible in practice, because in the case of fine-grained goods the area of existence shrinks, so that the permissible limits for the gas velocity during practical operation inevitably have to Over- resp. undercut. If, on the other hand, you work with coarse material, ie. with particle sizes of several mm size, this area can be practically realized, whereby the velocity of the bar gas in the nozzle, i.e. in the lower part of the apparatus amounting to about 40 m / sec, roughly corresponds to the maximum load, i.e. the top of the dotted curve. At even higher gas velocities and when using fine-grained material, ie. such as with particle sizes of about 1 mm, one enters the area C for the pneumatic transport. The pressure losses are also higher than at idle and parallel pressure loss curves are obtained for different feed speeds. If the gas velocity is too small, the material is not carried away and, as indicated by the punctured beginning of the pressure loss curves, one enters an unstable area.

Om nu i omradet A kemiska eller fysikaliska processer genomforas, tillf5res apparaten kontinuerligt virvelgods, vilket kan vara fast, flytande eller degigt. Stallet for inmatningen Or joke kritiskt och kan befinna sig langt ned eller vid apparatens Oversta dude. Uttagningen sker lampligen nedtill, men kan aven ske ungefar pa mitten av apparaten. Sarskilt fina delar av virvelgodset medryckas av gasstrommen och kunna pa kant satt avskiljas medelst en ansluten cyklon. Det är naturligtvis Oven mojligt, att aterfora dessa till behandlings- rummet, Pa detta satt kunna exempelvis sul- fidmalmer rostas. Vid antimonmalmer, vid vilka vid rostningen den uppstaende antimon- oxiden Or flyktig, kan t. ex. rostningen till och med ske Over smalttemperaturen. Det Or Oven mojligt att anordna flera dylika ventu- rivirvlare Over varandra och lata godset kontinuerligt falla frau det ena steget till det andra och darigenom under rostningen genomfora flerstegsprocesser, sasom t. ex. avdrivning av flyktiga sulfider. If chemical or physical processes are now carried out in area A, the apparatus is continuously supplied with swirl material, which can be solid, liquid or doughy. The input for the input Or joke is critical and can be located far down or at the device's Top dude. The removal is done at the bottom, but can also take place approximately in the middle of the appliance. Particularly fine parts of the vortex are entrained by the gas stream and can be separated at the edge by means of a connected cyclone. Of course, it is also possible to return these to the treatment room. In this way, for example, sulphide ores can be roasted. In the case of antimony ores, in which the roasting antimony oxide or volatile during roasting, e.g. roasting even takes place over the melting temperature. It is also possible to arrange several such ventricular vortices on top of each other and to let the goods continuously fall from one step to the other and thereby carry out multi-step processes during roasting, such as e.g. evaporation of volatile sulphides.

Genom tillforsel av f8rbranningsmaterial kunna hOga temperaturer erhallas och man kan t. ex. avsvavla blandningar av gips, kisel- syra och kol under bildning av en cementartad klinker. Det Or Oven m8jligt att anordna venturireaktorn Over en normal virvelskiktsreaktor och pa detta satt arbeta i tva steg. Aven kombinationen med en roterugn kan vara firirdelaktig. By supplying combustion material, high temperatures can be obtained and one can e.g. desulfurize mixtures of gypsum, silicic acid and carbon to form a cementitious tile. It is also possible to arrange the venturi reactor over a normal fluidized bed reactor and in this way work in two steps. Even the combination with a rotary kiln can be fatal.

En sarskild fordel med sattet enligt uppfinningen bestar dan, att man i motsats till den kanda virvelskikttekniken, vid vilken som bekant ytterst noga maste undvikas, att de fasta delarna bli klibbande eller till och med smalta, kan arbeta med klibbiga, degiga eller till och med flytande partiklar i suspensionen. Det ar salunda enligt uppfinningen mojligt att granulera i det fritt svavande virvelskiktet. Granuleringen kan t. ex. astadkommas pa sa vis, att ett annu smuligt fuktigt gods infores i en varm barargasstrom. A particular advantage of the method according to the invention is that, in contrast to the well-known vortex layer technique, in which, as is well known, extreme care must be avoided that the solid parts become sticky or even narrow, it is possible to work with sticky, doughy or even liquid particles in the suspension. Thus, according to the invention, it is possible to granulate in the free-floating vortex layer. The granulation can e.g. achieved in such a way that an otherwise crumbly moist goods is introduced into a hot bare gas stream.

Nedan forklaras ytterligare sattet enligt uppfinningen och nagra for dess genomfO- rande lampliga anordningar i saraband med atfOljande ritningar, p0 vilka fig. 2-6 schematiskt visa nagra utforings former av anordningar enligt uppfinningen. The method according to the invention and some of its implementable lamp devices are further explained below in conjunction with the accompanying drawings, in which Figures 2-6 schematically show some embodiments of devices according to the invention.

Fig. 2 visar en anordning for avrostning av sulfidmalmer medelst sattet enligt uppfin- ningen. Den bestar av en konisk, diffusorliknande del 1, i vilken den enligt uppfinningen svavande suspensianen av fasta kroppar gas befinner sig. Darover foljer en som broms- zon tjanande utvidgning 2 och ett inmurat schakt 3, i vilket de eventuellt hiigt uppblasta bestandsdelarna i den svavande badden kunna efterrostas effektivt. Under den koniska delen finnes ett munstycksliknande inlopp 4 med en slussanordning 5. De for rostningen nadvandiga syrehaltiga gaserna, vilka samtidigt tjana som biirargas, inledas i sidled vid 6 och lamna reaktorn vid 7. Den for avrostning avsedda sulfidmalmen forvaras i en ficka 8 och inmatas medelst en tallriksmatare i virvelbadden genom ett schakt 9. Vid 10 Or ett utmatningsror anordnat, som mynnar en slussanordning 11. Den koniska delen, i vilken reaktionen till stOrsta delen ager rum, Or forsedd med en kylmantel 12, genom vilken kylvatten kan inmatas vid 13 och utmatas vid 14. Med denna anordning kunna pa universellt satt sulfidmalmer avrostas. Avrostningen kan genomforas vid temperaturer under sintringspunkten, men i motsats mot kanda satt Or det icke nodvandigt att halla temperaturen under mjuknings- eller smallpunkten. Den medelst uppfinningen mojliga hOga rostningstemperaturen medger att hOgre rostningshastighet erhalles och darigenom en hogre ugnsbelastning kan uppra.tthallas. Dessutom Mir branderna samtidigt med avrostningen agglomeriserade, sA att den med gasen avforda delen Or finkornigare an den i de kanda virvelskikten erhallna. Den kan salunda nastan helt och hallet avlagsnas ur gasen medelst mekaniska stoftavskilj are. Fig. 2 shows a device for defrosting sulphide ores by means of the set according to the invention. It consists of a conical, diffuser-like part 1, in which the suspension of solids gas floating according to the invention is located. This is followed by an extension 2 serving as a brake zone and a built-in shaft 3, in which the possibly highly inflated components in the floating bath can be roasted efficiently. Below the conical part there is a nozzle-like inlet 4 with a locking device 5. The oxygen-containing gases present for roasting, which at the same time serve as secondary gas, start laterally at 6 and leave the reactor at 7. The sulphide ore intended for roasting is stored in a pocket 8 and fed by means of a plate feeder in the whirlpool bath through a shaft 9. At 10 Or a discharge pipe arranged, which opens a lock device 11. The conical part, in which the reaction for the most part takes place, Or provided with a cooling jacket 12, through which cooling water can be fed at 13 and discharged at 14. With this device, sulphide ores can be rusted in a universal way. The defrosting can be carried out at temperatures below the sintering point, but in contrast to the kanda, it was not necessary to keep the temperature below the softening or narrowing point. The high roasting temperature possible by means of the invention allows a higher roasting speed to be obtained and thereby a higher oven load can be maintained. In addition, at the same time as the defrosting, the fires agglomerated, so that the part removed with the gas was finer grained than that obtained in the known vortex layers. It can thus be almost completely and the hall removed from the gas by means of mechanical dust collectors.

I fig. 3 visas en anordning for rostning i mellansteg, exempelvis avrostning av blyhaltiga zinkmalmer under samtidigt avlagsnande av blyet ur rostgodset. Den bestar av en sig vidgande del 15, i vilken exempelvis den blyhaltiga zinksulfiden inmatas genom ett rOr 17 och Mlles i svavande tillstand. Ovanfor den koniska delen 15 f8ljer ett cylindriskt schakt 16, i vilket de med barargasen eventuellt Mgt upp medforda partiklarna kunna slutreagera. Som barargas genomledes het och praktiskt taget syrefri rostgas, som kommer frail anordningens undre del. I denna heta, syrefria gasstrom forflyktigas blyet som sulfid. Den blyfria zinksulfiden ledes Over ett .braddavlopp 18 forbi eventuellt automatiskt reglerade slussanordningar 19 genom ett schakt 20 till en undre konisk del 21. Med hjalp av den syrehaltiga bargasen sker har avrostning till zinkoxid pa nyss beskrivet sat. Ovanfor den koniska delen 21 finnes aterigen ett eylindriskt schakt 22, i vilket de Mgt upp medforda sulfidpartiklarna kunna underga efterrostning. Utmatningen kan antingen fiirsigga Over ett braddavlopp 25 eller genom en munstycksliknande utvidgning 23 och en slussanordning 24. Bargasen inledes vid 26 och lamnar apparaturen vid 27, varifran den ledes f8rbi en avgaspanna och an kylanordning till en elektrisk gasrenare, I vilken blysulfiden kan avskiljas. Det Or 4— — emellertid aven mojligt att genom fornyad syretillfOrsel forbranna blysulfiden i en efterforbranningskamm are och utvinna ett oxidstoft. Den enligt uppfinningen foreslagna tvastegsapparaten uppvisar stora fordelar i jamf8re1se med de kanda, i tvâ steg arbetande flytbaddsreaktorerna genom att medge att 1) sa h5ga temperaturer uppnas i den undre rostugnen, att den klibbiga beskickningen knappast langre visar tendens att damma, och 2) inga igensattningar kunna langre intrada i ovre delen som foljd av i undre delen bildat stoft, vilket sasom kant ofta är fallet vid de med roster eller munstycksbottnar fOrsedda flytbaddsugnarna. Fig. 3 shows a device for roasting in intermediate stages, for example roasting of lead-containing zinc ores while simultaneously removing the lead from the roasting material. It consists of an expanding part 15, in which, for example, the lead-containing zinc sulphide is fed through a tube 17 and Mlles in a floating state. Above the conical part 15 follows a cylindrical shaft 16, in which they can finally react with the bar gas, possibly carrying the particles upwards. As bare gas, hot and practically oxygen-free rust gas is passed through, which comes from the lower part of the device. In this hot, oxygen-free gas stream, lead is volatilized as sulfide. The unleaded zinc sulphide is led over a brad drain 18 past any automatically regulated locking devices 19 through a shaft 20 to a lower conical part 21. With the aid of the oxygen-containing bark gas, de-roasting to zinc oxide takes place in the manner just described. Above the conical part 21 there is again a cylindrical shaft 22, in which the sulphide particles which may be carried up can undergo post-rusting. The discharge can either flow over a barbed drain 25 or through a nozzle-like extension 23 and a locking device 24. The bare gas is introduced at 26 and leaves the apparatus at 27, from where it is led past an exhaust boiler and cooling device to an electric gas purifier in which lead sulphide can be separated. However, it is also possible to burn the lead sulphide in a post-combustion chamber by renewed oxygen supply and to recover an oxide dust. The two-stage apparatus proposed according to the invention has great advantages in comparison with the known, two-stage floating bath reactors by allowing 1) such high temperatures to be reached in the lower roasting furnace that the sticky charge hardly shows any tendency to dust, and 2) no obstructions. be able to insert longer in the upper part as a result of dust formed in the lower part, which as an edge is often the case with the floating bath ovens provided with grids or nozzle bottoms.

Pa grund harav ãr det aven mojligt att utbilda den undre delen som vanlig flytbaddseller virvelskiktsugn och endast anordna den byre delen som svavbaddsreaktor. Due to this, it is also possible to train the lower part as an ordinary floating bath or vortex layer furnace and only arrange the upper part as a sulfur bath reactor.

I fig. 4 visas en kombination av den enligt uppfinningen fOrelagna svavbaddsreaktorn med en roterugn. Anordningen bestar av en roterugn 28, vilken kan hallas nagot kortare an vad fallet vanligtvis är yid roterugnar, och I vilken lamplige,n skovelliknande omrorare aro anordnade. Behandlingsgodset beskickas roterugnen vid 29, genomvandrar denna och rinner ned i en slusslada 30, som eventuellt oppnas och stanges automatiskt, och kommer darifran genom ett fallrEir 31 ned i den koniska delen 32 av en svavbaddsreaktor, som aterigen är forsedd med ett efterreaktionssehakt 33, en braddavloppsutmatning 34, och godsutmatning 35-36. Barargasen tillfores svavbaddsreaktorn vid 37 och lamnar den vid 38. FOrdelen med denna kombination av svavbaddsreaktor och roterugn bestar framfor alit dari, att varmeinnehallet hos de gaser, som lamna svavbaddsreaktorn, i star utstrackning kan tillgodogoras f8r sjalva reaktionen i roterugnen. Verlmingssattet ka,n forklaras genom en beskrivning av forfarandets tillampning vid utdragning av tenn ur pyritkoncentrat. De tennhaltiga pyritkoncentraten tillfaras roterugnen 28 vid 29. Dar komma de i intim beroring med fran svavbaddsreaktorn harrorande, heta rostgaser, varigenom en blandning av svavel och tennsulfid avdestillerar. Det frAn roterugnen utmatade godset, som praktiskt taget bestar av bildad pyrrhotit, kommer Over ett fallror 31 in i flytbaddsreaktorn och avrostas dar till Fe2O3 med syrehaltiga gaser, varvid man kan ga synnerligen Mgt med rosttemperaturen. Den vid 38 avgaende blandningen av svavelanga och tennsulfid kan darpa, eventuellt efter en efterforbranning, bearbetas enligt kanda metoder, varvid tennsulfiden kan utvinnas direkt eller eventuellt erhallas som cecid. Apparatens varmehushallning gar med fordel att reglera darigenom, att en del av den fran tenn befriade avgasen vid 37 till-Ores svo.vbaddsreaktorn, dar den upptager det overskott av reaktionsvarmet, som eljest vid vanliga rostningsforlopp skulle ha avlagsnats genom kylning, och tillfores beskickningen i roterugnen. I denna anordning ar det aven mojligt att avrosta pyriter delvis med direkt utvinning av svavlet. Det kan ofta vara fordelaktigt att inbygga en dylik svavbaddsreaktor i redan forefintliga roterugnsanlaggningar, varigenom det blir mojligt att uppna. en avsevard effektokning hos roterugnen. Fig. 4 shows a combination of the sulfur bath reactor presented according to the invention with a rotary kiln. The device consists of a rotary kiln 28, which can be held somewhat shorter than is usually the case with rotary kilns, and in which lamp-like, paddle-like stirrers are arranged. The treatment material is loaded into the rotary kiln at 29, traverses it and flows down into a sluice barn 30, which may be opened and closed automatically, and comes therefrom through a falling wire 31 down into the conical part 32 of a sulfur bath reactor, which is again provided with a post-reaction shaft 33, a brad drain discharge 34, and goods discharge 35-36. The bar gas is fed to the sulfur bath reactor at 37 and leaves it at 38. The advantage of this combination of sulfur bath reactor and rotary kiln is that the heat content of the gases leaving the sulfur bath reactor can to a large extent be credited for the actual reaction in the rotary kiln. The method of heating can be explained by a description of the application of the process when extracting tin from pyrite concentrate. The tin-containing pyrite concentrates are fed to the rotary kiln 28 at 29. There they come into intimate contact with hot rust gases bubbling from the sulfur bath reactor, whereby a mixture of sulfur and tin sulphide distills off. The goods discharged from the rotary kiln, which practically consists of formed pyrrhotite, enters a floating bath reactor 31 via a trap tube and is defrosted there to Fe 2 O 3 with oxygen-containing gases, whereby the rust temperature can be very high. The mixture of sulfuric acid and tin sulphide leaving at 38 can be darpa, possibly after an afterburning, processed according to known methods, whereby the tin sulphide can be recovered directly or possibly obtained as a cecide. The heat storage of the apparatus can advantageously be regulated in that a part of the exhaust gas liberated from the tin at the 37 to-Ore soaking bath reactor, where it absorbs the excess heat of reaction, which would otherwise have been removed by cooling during normal roasting processes, and is fed to the charge in roterugnen. In this device it is also possible to partially defrost pyrites with direct extraction of the sulfur. It can often be advantageous to incorporate such a sulfur bath reactor in already existing rotary kiln plants, thereby making it possible to achieve. a significant increase in power in the rotary kiln.

En annan fordelaktig tillampning av del enligt uppfinningen foreslagna forfarandet kan ske i en anordning, som visas schematiskt i fig. 5. Denna svavbaddsreaktor bestar av en konisk del 39, 1 vilken svavbadden utbiIdas, ett efterbehandlingsschakt 40 och ett inloppsmunstyeke 41. Vid 42 bar anordnats en utmatning for granulatet. Barargasen inf8res vid 43 och lamnar anordningen vid 44. Vid 45 och 46 kunna olika fasta eller flytande medier inmatas, medan vid 47 i vissa fall utmatning kan goras direkt ur svavbadden. Derma anordning lampar sig sarskilt for utforande av varmekonsumerande reaktioner, vid vilka ett bransle, t. ex. kol, tillfOres. Slutprodukten kan harvid som sintrat eller osintrat material avlagsnas fran svavbadden genom utmatningen 47 eller genom redan tidigare beskrivna utmatningar. Pa detta satt ar det t. ex. mi5jligt att branna resp. kalcinera cement, kalk, dolomit, sulfat, silikat, fosfat, bauxit osv. Harvid inmatas materialet foretradesvis vid 45, medan branslet t. ex. kol, exempelvis inslussas vid 46. Som barargas kan man anvanda luft men aven med f8rdel rent syre eller syreanrikad luft. Another advantageous application of the part proposed according to the invention can take place in a device, which is shown schematically in Fig. 5. This sulfur bath reactor consists of a conical part 39, in which the sulfur bath is formed, a finishing shaft 40 and an inlet nozzle 41. At 42 bar a discharge for the granulate. The bar gas is introduced at 43 and leaves the device at 44. At 45 and 46 different solid or liquid media can be fed, while at 47 in some cases discharge can be made directly from the sulfur bath. This device is particularly suitable for carrying out heat-consuming reactions in which a branch, e.g. coal, supplied. The final product can then be removed from the sulfur bath as sintered or unsintered material through the discharge 47 or through discharges already previously described. In this way it is e.g. possible to burn resp. calcine cement, lime, dolomite, sulphate, silicate, phosphate, bauxite, etc. In this case, the material is preferably fed at 45, while the industry e.g. carbon, for example, is contained at 46. Air can be used as bare gas, but also with the benefit of pure oxygen or oxygen-enriched air.

I fig. 6 visas en anordning for granulering av finfordelade amnen. Genom en mataranordning 48 inmatas exempelvis en annu smuHg blandning av kiselgur och vattenglas i ett sig vidgande sehakt 49. Har utbildas en svavbadd med hjalp av en vid 50 inledd strom av en c:a 350° C varm barargas. Genom ett spridningsmunstycke 51 infores t. ex. svavelsyra i finfordelad form i svavbadden. Svavelsyran astadkommer en granulering av smulprodukten, som i form av mycket likformiga kulor redan torra sjunka nedat och kunna utmatas vid 52. Ovanfor svavbadden ar en utvidgning 53 anordnad, i vilken Mgt uppkastade partiklar separeras. For fullstandig avdamning her det dessutom anordnats en stoftavskiljare 54 fore gasavloppet 55. De bildade kulorna aro nagot porosa och lampa sig hi. a. som barare for katalysatorsub stanser. Fig. 6 shows a device for granulating finely divided blanks. By means of a feeding device 48, for example, an annu smhUg mixture of diatomaceous earth and water glass is fed into a widening shaft 49. A sulfur bath has been formed with the aid of a stream of about 350 ° C hot gas started at 50. Through a spreading nozzle 51, e.g. sulfuric acid in finely divided form in the sulfur bath. The sulfuric acid produces a granulation of the crumb product, which in the form of very uniform spheres already dries downwards and can be discharged at 52. Above the sulfur bath an extension 53 is arranged, in which highly vomited particles are separated. For complete evaporation, a dust collector 54 has also been arranged in front of the gas drain 55. The formed balls are slightly porous and light up. a. as a bar for catalyst substances.

Claims

Patent claim Ak:

Set to continuously carry out chemical and / or physical reactions between solid and / or liquid particles 0. one side and a treatment gas or steam A other - - side in swirling suspension in an upwardly expanding, stainless, diffuser-shaped treatment room during supply of gas from below, characterized in that the gas velocity is caused to decrease upwards Trier corresponding to the square of the elevation, so that the gas stream atnainstone over a significant part of the hold does not slacken the cradle and a free floating swirling suspension with pronounced free lower spruce surface is formed. the material to be treated is installed so that particles falling out of the space filled by the suspension fall down through the gas stream and that the main mass of the solid material is not carried out of the gas upwards out of the treatment room.

2. A kit according to claim 1, characterized in that in the suspension liquid and / or sticky particles are treated, possibly for agglomeration into larger grains.

3. Set according to claims 1 and 2, characterized in that the treatment gas is supplied laterally in the reactor under the inlet nozzle. Anfarda Publications: Patentskrifter iron Sverige 92547; Belgium 493488, 493489; Great Britain 285 038; USA 2,445,327, 2,456,796, 2,475,607.