NO166621B - PROCEDURE FOR SEPARATING SOLID SUBSTANCES FROM SOLID SUSPENSIONS. - Google Patents
PROCEDURE FOR SEPARATING SOLID SUBSTANCES FROM SOLID SUSPENSIONS. Download PDFInfo
- Publication number
- NO166621B NO166621B NO870642A NO870642A NO166621B NO 166621 B NO166621 B NO 166621B NO 870642 A NO870642 A NO 870642A NO 870642 A NO870642 A NO 870642A NO 166621 B NO166621 B NO 166621B
- Authority
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- Norway
- Prior art keywords
- filter
- pressure
- suspension
- pressure vessel
- solids
- Prior art date
Links
- 239000000725 suspension Substances 0.000 title claims description 48
- 238000000034 method Methods 0.000 title claims description 22
- 239000007787 solid Substances 0.000 title claims description 21
- 239000000126 substance Substances 0.000 title 1
- 238000001914 filtration Methods 0.000 claims description 24
- 239000012065 filter cake Substances 0.000 claims description 20
- 238000007791 dehumidification Methods 0.000 claims description 6
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 4
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 239000000049 pigment Substances 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 2
- 239000004408 titanium dioxide Substances 0.000 claims description 2
- 239000002699 waste material Substances 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 description 18
- 239000000706 filtrate Substances 0.000 description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 238000000926 separation method Methods 0.000 description 4
- 230000035939 shock Effects 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000011085 pressure filtration Methods 0.000 description 2
- 241000446313 Lamella Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- -1 it can. steam Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229910021653 sulphate ion Inorganic materials 0.000 description 1
- 238000003828 vacuum filtration Methods 0.000 description 1
Classifications
-
- 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
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/90—Separation; Purification
- C01B17/901—Recovery from spent acids containing metallic ions, e.g. hydrolysis acids, pickling acids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/11—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements
- B01D29/114—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements arranged for inward flow filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/76—Handling the filter cake in the filter for purposes other than for regenerating
- B01D29/80—Handling the filter cake in the filter for purposes other than for regenerating for drying
- B01D29/84—Handling the filter cake in the filter for purposes other than for regenerating for drying by gases or by heating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/88—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices
- B01D29/90—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices for feeding
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D35/00—Filtering devices having features not specifically covered by groups B01D24/00 - B01D33/00, or for applications not specifically covered by groups B01D24/00 - B01D33/00; Auxiliary devices for filtration; Filter housing constructions
- B01D35/16—Cleaning-out devices, e.g. for removing the cake from the filter casing or for evacuating the last remnants of liquid
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Filtration Of Liquid (AREA)
- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
- Treatment Of Sludge (AREA)
- Preparation Of Clay, And Manufacture Of Mixtures Containing Clay Or Cement (AREA)
Description
Oppfinnelsen vedrører en fremgangsmåte til adskillelse av faste stoffer fra faststoffrike suspensjoner ved diskontinuerlig filtrering i trykkfiltre. The invention relates to a method for separating solids from solids-rich suspensions by discontinuous filtration in pressure filters.
Faststoffrike suspensjoner kan adskilles ved vakuum- eller overtrykkfiltrering. Vanligvis foretrekkes den kontinuerlige vakuumfiltrering, eventuelt med Precoat-sjikt for oppnåelse av en akseptabel filterytelse (Ullmanns Enzyklopadie d. techn. Chemie, Verlag Chemie, Weinheim, 4. opplag, 1972, bind 2, s. 188 ff). Suspensions rich in solids can be separated by vacuum or positive pressure filtration. Continuous vacuum filtration is usually preferred, possibly with a Precoat layer to achieve an acceptable filter performance (Ullmann's Enzyklopadie d. techn. Chemie, Verlag Chemie, Weinheim, 4th edition, 1972, volume 2, p. 188 ff).
Suspensjoner av meget findelte faststoffer gir imidlertid ofte så små filterytelser at faststoffadskillelsen må foregå ved trykkfiltrering. For dette formålet har filterpresser vist seg egnede. Disse har imidlertid ulempen med høye spesifikke apparatkostnader, fordi ved liten automatiserings-grad utgjør varigheten for tømming av filterpressen, spesielt ved filtrering av faststoffrike suspensjoner, en vesentlig del av den samlede chargevarighet eller ved høy automati-seringsgrad er de absolutte apparatomkostninger meget høye. Suspensions of very finely divided solids, however, often give such low filter performances that the solids separation must take place by pressure filtration. For this purpose, filter presses have proven to be suitable. However, these have the disadvantage of high specific device costs, because with a low degree of automation the duration for emptying the filter press, especially when filtering suspensions rich in solids, constitutes a significant part of the overall batch duration or with a high degree of automation the absolute device costs are very high.
Vesentlig gunstigere ligger de til filterflaten refererte spesifikke apparatomkostninger ved trykkfiltre av typen blad-eller patronfilter. Disse filtre har imidlertid den ulempe at ved hver charge må et stort beholdervolum før den egentlige filtrering fylles med suspensjon og etter filtrering tømmes. Ved suspensjoner, som f.eks. inneholder 10 vekt-eller mer faststoffer og som alt etter trykk og gjennom-trengelighet av filterkaken, fører til korte filtreringstider fra sekunder til noen få minutter, får den forholdsvis lange varighet av fylling og tømming av filtre med suspensjonen stor betydning. Ved suspensjoner med minst 10 vekt-$ fast-stoffinnhold utgjør filterhusets volum alt etter faststoff-innhold 1 til 10 ganger av det pr. charge dannede filtrat-volum. For å oppnå korte fylltider er det derfor nødvendig med meget store, omstendelige pumper. Dessuten medfører den hyppige inn- og utkobling av slike pumper betraktelige problemer. Dertil kommer at ved den gjentatte transport av suspensjonen med pumper ødelegges faststoffpartiklene selv eller agglomerater av disse og derved blir filtrerbarheten dårligere og avfuktningen av filterkaken vanskeliggjøres. Av disse grunner kommer tidligere trykkfiltre av typen blad-eller patronfiltre knapt til anvendelse for filtrering av faststoffrike suspensjoner, spesielt ikke når filtreringen også er mulig med kontinuerlig arbeidende vakuumfiltre. The specific device costs referred to the filter surface are significantly more favorable for pressure filters of the leaf or cartridge filter type. However, these filters have the disadvantage that with each charge a large container volume must be filled with suspension before the actual filtration and emptied after filtration. In the case of suspensions, such as contains 10 by weight or more solids and which, depending on the pressure and permeability of the filter cake, leads to short filtration times from seconds to a few minutes, the relatively long duration of filling and emptying filters with the suspension is of great importance. For suspensions with at least 10% solids content by weight, the volume of the filter housing is, depending on the solids content, 1 to 10 times that per charge formed filtrate volume. In order to achieve short filling times, very large, cumbersome pumps are therefore necessary. In addition, the frequent switching on and off of such pumps causes considerable problems. In addition, during the repeated transport of the suspension with pumps, the solid particles themselves or agglomerates of these are destroyed and thereby the filterability becomes worse and the dehumidification of the filter cake becomes more difficult. For these reasons, previous pressure filters of the blade or cartridge filter type are hardly used for filtering suspensions rich in solids, especially not when the filtering is also possible with continuously working vacuum filters.
Oppfinnelsens oppgave var derfor å tilveiebringe en fremgangsmåte som ikke har de ovennevnte ulemper under samtidig utnyttelse av trykkfilterets fordeler. The task of the invention was therefore to provide a method which does not have the above-mentioned disadvantages while simultaneously utilizing the advantages of the pressure filter.
Overraskende ble det nå funnet at dette er mulig når fyllingen av trykkfilteret likeledes som den egentlige filtrering, foregår fra en separat trykkbeholder, hvori også suspensjonen tømmes etter foregått filtrering. Surprisingly, it was now found that this is possible when the filling of the pressure filter, as well as the actual filtration, takes place from a separate pressure vessel, in which the suspension is also emptied after filtration.
Foreliggende oppfinnelse vedrører følgelig en fremgangsmåte til adskillelse av faststoffer fra faststoffrike suspensjoner ved diskontinuerlig filtrering i trykkfiltre, hvori suspensjonen transporteres pneumatisk fra en trykkbeholder. Fremgangsmåten er kjennetegnet ved at den overskytende suspensjonen etter frembringelse av filterkaken på filtermediet pneumatisk tilbaketransporteres til trykkbeholderen ved hjelp av trykkgass, at det med den for pneumatisk tømming av filteret benyttede trykkgassen samtidig foregår en fjernelse av fuktighet fra filterkaken og at suspensjonsrester etter avsluttet kake-avfukting pneumatisk fjernes fra filteret før den avfuktede filterkaken tas ut. The present invention therefore relates to a method for separating solids from suspensions rich in solids by discontinuous filtration in pressure filters, in which the suspension is transported pneumatically from a pressure vessel. The method is characterized by the fact that, after producing the filter cake on the filter medium, the excess suspension is pneumatically transported back to the pressure vessel with the help of compressed gas, that the compressed gas used for pneumatically emptying the filter simultaneously removes moisture from the filter cake and that suspension residues after the cake dehumidification is completed pneumatically removed from the filter before the dehumidified filter cake is removed.
Spesielt foretrukket er derved den fremgangsmåtevariant hvor volumet av trykkbeholderen er minst 10%, fortrinnsvis 10-10056 større enn volumet av trykkfilteret. Particularly preferred is the process variant where the volume of the pressure vessel is at least 10%, preferably 10-10056 greater than the volume of the pressure filter.
Fremgangsmåten ifølge oppfinnelsen forklares i det følgende under henvisning til figuren, hvor det er vist en mulig anordning til gjennomføring av fremgangsmåten Ifølge oppfinnelsen. The method according to the invention is explained below with reference to the figure, where a possible device for carrying out the method according to the invention is shown.
Anordningen består av et trykkfilter 1 av typen blad- eller patronfilter, en dermed forbundet trykkbeholder 2, hvis volum minst er 10%, fortrinnsvis minst 50% større enn volumet av trykkfilteret, en pumpe 3 til innmating av suspensjonen i trykkbeholderen 2, et skilleapparat 4 til adskillelse av filtratet fra den til kakeavfuktning benyttede gass og et skilleapparat 5 til adskillelse av restsuspensjonen fra gassen, hvormed denne rest trykkes ut av filteret. Som skilleapparat 4 kan det alt etter type og dråpestørrelse av filtratet medrevet med den for avfuktning gjennom filterkaken førte gass, komme til anvendelse enkle kar, cyklonutskillere, lamellutskiUere, trådnettutskillere, filtre, EGR'er eller andre kjente skilleapparater. Skilleapparatet 5 kan eventuelt utelates når resttømmingen føres inne i trykkbeholderen 2. The device consists of a pressure filter 1 of the leaf or cartridge filter type, a connected pressure vessel 2, the volume of which is at least 10%, preferably at least 50% greater than the volume of the pressure filter, a pump 3 for feeding the suspension into the pressure vessel 2, a separator 4 for separating the filtrate from the gas used for cake dehumidification and a separator 5 for separating the residual suspension from the gas, with which this residual is pressed out of the filter. Depending on the type and droplet size of the filtrate, simple vessels, cyclone separators, lamella separators, wire mesh separators, filters, EGRs or other known separators can be used as separator 4. The separating device 5 can optionally be omitted when the residual emptying is carried inside the pressure vessel 2.
Suspensjonen 26 transporteres med pumpen 3 med en ved hjelp av reguleringsarmatur 13 innstilt transportytelse inn i trykkbeholderen 2 som tilsvarer den gjennomsnittlige filtreringsytelse av den diskontinuerlige prosess. Fra den fylte trykkbeholder 2 trykkes suspensjonen diskontinuerlig ved hjelp av trykkgass 25 gjennom forbindelsesledningen 27 inn i filteret 1. Gasstrykket opprettholdes inntil filteret 1 er fylt og på filtermidlet er frembragt en filterkake av den tilsiktede tykkelse. Som trykkgass kan det ved oppfinnelsen anvendes enhver gass som forholder seg inert ovenfor suspensjonen som skal filtreres. En foretrukket gass er luft. The suspension 26 is transported by the pump 3 with a transport performance set by means of the control armature 13 into the pressure vessel 2 which corresponds to the average filtration performance of the discontinuous process. From the filled pressure vessel 2, the suspension is discontinuously pressed with the help of compressed gas 25 through the connection line 27 into the filter 1. The gas pressure is maintained until the filter 1 is filled and a filter cake of the intended thickness is produced on the filter medium. Any gas which is inert to the suspension to be filtered can be used as pressurized gas in the invention. A preferred gas is air.
Alt etter sammensetningen av suspensjonen kan det imidlertid også. anvendes damp, nitrogen, argon, karbondioksyd, helium og andre lett tilgjengelige gasser. However, depending on the composition of the suspension, it can. steam, nitrogen, argon, carbon dioxide, helium and other readily available gases are used.
Det ved denne filtrering dannede filtrat 16 kommer gjennom den åpnede avsperringsarmatur 8 inn i skilleapparatet 4, hvorfra det renner bort i en filtratbeholder. The filtrate 16 formed by this filtration comes through the opened shut-off fitting 8 into the separator 4, from where it flows away into a filtrate container.
Etter forløp av den for oppnåelse av den tilsiktede kake-tykkelse nødvendige filtreringstid lukkes avsperringsarmaturen 12 og avsperringsarmaturen 6 åpnes, hvorigjennom trykkgass 14 trer inn i suspensjonssiderommet av filteret 1. Ved hjelp av trykkgassen kan eventuelt suspensjonen dessuten filtreres så vidt som filterblader eller filterpatroner dypper inn i suspensjonen. Deretter kan suspensjonen i den nedre del av filteret 1 over ledningen 27 tilbaketransporteres i trykkbeholderen 2, idet det fra trykkbeholderen 2 gjennom avsperringsarmaturen 11 fjernes trykkgass 24. Da ved denne prosess filterkaken i den nedre del av filteret 1 oppnår en tydelig større tykkelse enn i den øvre del av filteret 1, foretrekkes for de faststoffrike suspensjoner følgende prosess: Etter åpning av avsperringsarmaturen 6 åpnes avsperringsarmaturen 11 således at suspensjonen strømmer bort over ledning 27 i løpet av kort tid, men uten trykkstøt til trykkbeholderen 2. Den gjennom avsperringsarmaturen 6 innmatede trykkgass 14 bevirker for det første uttrykking av suspensjonen fra filteret 1, for det annet filtrering av en liten del av suspensjonen, hvori filterelementene enda dypper inn under den hurtige tømming og for det tredje avfukting av filterkaken. Den innmatede trykkgass 14 unnviker sammen med den medrevne fuktighet gjennom den åpnede avsperrearmatur 8 inn i skilleapparatet 4, hvori det foregår skilling i filtrat 18 og avgass 19. Etter tilstrekkelig avfukting av filterkaken åpnes avsperringsarmaturen 9 og den resterende suspensjon 21 trykkes fra filteret 1. I skillekaret 5 foregår adskillelsen av suspensjonen 22 fra trykkgassen 20. Etter fjerning av den resterende suspensjon 21 lukkes avsperringsarmaturen 6, avsperringsarmaturen 10 åpnes og filterkaken 23 taes ut fra filteret 1. Ved bladfilteret foregår kake-avkasting av filtermidlet på kjent måte, fortrinnsvis ved rotasjon eller vibrering av bladene. Ved de spesielt foretrukne patronfiltre foregår kakeuttaket ved lukking av avsperringsarmaturen 8 og støtvis innblåsing av trykkgass 15 inn i filtratledningen ved plutselig åpning av avsperringsarmaturen 7. After the filtration time required to achieve the intended cake thickness has elapsed, the shut-off fitting 12 is closed and the shut-off fitting 6 is opened, through which pressurized gas 14 enters the suspension side space of the filter 1. With the help of the pressurized gas, the suspension can also be filtered as far as filter blades or filter cartridges dip in the suspension. The suspension in the lower part of the filter 1 can then be transported back into the pressure vessel 2 via the line 27, as pressurized gas 24 is removed from the pressure vessel 2 through the shut-off fitting 11. Then, in this process, the filter cake in the lower part of the filter 1 achieves a distinctly greater thickness than in the upper part of the filter 1, the following process is preferred for suspensions rich in solids: After opening the shut-off fitting 6, the shut-off fitting 11 is opened so that the suspension flows away via line 27 within a short time, but without a pressure shock to the pressure vessel 2. The pressurized gas 14 fed through the shut-off fitting 6 causes, firstly, expression of the suspension from the filter 1, secondly, filtering of a small part of the suspension, into which the filter elements still dip during the rapid emptying, and thirdly, dehumidification of the filter cake. The fed compressed gas 14 escapes together with the entrained moisture through the opened shut-off fitting 8 into the separator 4, in which separation takes place into filtrate 18 and exhaust gas 19. After sufficient dehumidification of the filter cake, the shut-off fitting 9 is opened and the remaining suspension 21 is pressed from the filter 1. In the separation vessel 5, the separation of the suspension 22 from the pressurized gas 20 takes place. After removal of the remaining suspension 21, the shut-off fitting 6 is closed, the shut-off fitting 10 is opened and the filter cake 23 is removed from the filter 1. With the leaf filter, cake ejection of the filter medium takes place in a known manner, preferably by rotation or vibration of the leaves. With the particularly preferred cartridge filters, the cake removal takes place by closing the shut-off fitting 8 and the sudden blowing of pressurized gas 15 into the filtrate line when the shut-off fitting 7 is suddenly opened.
Ved det foretrukne patronfilteret medfører den på figuren viste dypere oppstilling av trykkbeholderen 2 i forhold til filteret 1, spesielle fordeler, fordi derved er det i forbindelsesledning 27 ikke nødvendig med en avsperringsarmatur og sjokk unngås som kunne opptre ved den plutselige utstrømming av suspensjonen fra filteret 1 ved åpning av en så stor armatur. Disse sjokk kunne føre til nedfalling av en del av filterkaken fra filterpatroner og dermed til en følsom forstyrrelse av prosessen. Ved anordningen som anvendes ved oppfinnelsen med lavere oppstilling av trykkbeholderen 2 og regulert filtertømming ved avspenning av trykkbeholderen over avsperrearmaturen 11 unngås slike prosessforstyrreiser. In the case of the preferred cartridge filter, the deeper arrangement of the pressure vessel 2 in relation to the filter 1 shown in the figure brings special advantages, because there is no need for a shut-off fitting in the connection line 27 and shocks that could occur from the sudden outflow of the suspension from the filter 1 are avoided when opening such a large fixture. These shocks could lead to the fall of part of the filter cake from filter cartridges and thus to a sensitive disturbance of the process. With the device used in the invention with a lower arrangement of the pressure vessel 2 and regulated filter emptying by releasing the pressure vessel above the shut-off fitting 11, such process disturbances are avoided.
Spesielt foretrukket er således utførelsesformen av fremgangsmåten hvor trykkbeholderen er anordnet under trykkfilteret. Particularly preferred is thus the embodiment of the method where the pressure vessel is arranged below the pressure filter.
Ved filtrering av suspensjoner som gir godt vedhengende filterkaker eller ved anvendelse av bladfiltre, kan oppstillingen av filteret 1 og trykkbeholderen 2 på samme nivå by på fordeler. Oppstillingen, som krever innbygning av en avsperringsarmatur i ledningen 27, ligger innen rammen av oppfinnelsen, idet også derved foregår den hurtige fylling og tømming av filteret uten anvendelse av pumper. When filtering suspensions that give well-adherent filter cakes or when using leaf filters, positioning the filter 1 and the pressure vessel 2 at the same level can offer advantages. The set-up, which requires the installation of a shut-off fitting in the line 27, is within the scope of the invention, as it also enables the rapid filling and emptying of the filter without the use of pumps.
Filtreringen gjennomføres fordelaktig alltid således at under fyllingen av trykkfilteret og under filtrering er.trykket i trykkbeholderen høyere enn i trykkfilteret. The filtration is advantageously always carried out so that during the filling of the pressure filter and during filtration the pressure in the pressure vessel is higher than in the pressure filter.
Spesielle fordeler medfører oppfinnelsen ved filtrering av faststoffrike suspensjoner slik de fremkommer ved frem-stillingen av pigmenter, f.eks. av jernoksyd- og titandioksydpigmenter eller ved adskillelse av metallsalter fra svovelsyre innen rammen av en avfallssyreopparbeidelse. Special advantages result from the invention when filtering suspensions rich in solids as they appear during the production of pigments, e.g. of iron oxide and titanium dioxide pigments or by separating metal salts from sulfuric acid within the framework of a waste acid treatment.
I de tilfeller opprettholdes med gode resultater trykket i trykkbeholderen under filtreringen så lenge, eller eventuelt økes, inntil den krevede filterkaketykkelse på 15 til 50 mm er nådd. In those cases, the pressure in the pressure vessel during filtration is maintained with good results, or possibly increased, until the required filter cake thickness of 15 to 50 mm is reached.
Fordelene ved fremgangsmåten ifølge oppfinnelsen skal tydeliggjøres ved hjelp av et eksempel. The advantages of the method according to the invention shall be made clear by means of an example.
Eksempel Example
Det ble anvendt et "Fundabac"-patronfilter 1 fra firmaet DrM (Sveits) med en filterflate på 25 m<2> og et volum på 10 mJ . Pr. charge ble det filtrert 5 tonn (tilsvarende 2,9 m5 ) av en suspensjon av 1,38 t metallsulfat i 3,62 t 65$-ig svovelsyre. Varigheten av en charge utgjorde 16 minutter, så det fremkom en filterytelse på 18,75 t suspensjon/time. A "Fundabac" cartridge filter 1 from the company DrM (Switzerland) with a filter surface of 25 m<2> and a volume of 10 mJ was used. Per charge, 5 tonnes (equivalent to 2.9 m5 ) of a suspension of 1.38 t metal sulphate in 3.62 t 65% sulfuric acid were filtered. The duration of one charge was 16 minutes, so a filter performance of 18.75 t suspension/hour was obtained.
Trykkbeholderen 2 hadde et volum på 16 m5 . Den ble før begynnelsen av filtrering ved hjelp av pumpe 3 (transportytelse: 12 m> ved 8 bar mottrykk) 80% fylt med suspensjon 26. Ved begynnelsen av filtreringen ble det ved hjelp av reguler-ingsventil 12 innstilt en mengdestrøm på 10,7 m<5> suspensjon/ time. Filteret 1 ble i løpet av 2 minutter fylt fra behol-deren 2, idet suspensjonen ble trykket med trykkluft 25 på 7 bar gjennom ledning 27 inn i filteret 1. Volumstrømmen gjennom ledning 27 tilsvarte derved 300 m<5>/t. Etter fylling av filteret 1 og fortrenging av luft fra filteret 1 foregikk den egentlige filtrering umiddelbart. I løpet av 90 sekunder ble det filtrert 2,9 m<*> suspensjon, tilsvarende en volumstrøm på 116 m'/t gjennom lédning 27. Etter til sammen 3,5 minutter ble ventil 12 lukket, ventil 6 åpnet (innmating av trykkluft med 7 bar) og trykkbeholderen 2 ble avspent ved langsom åpning av ventilen 11. Ved oppnåelse av minimalstanden av suspensjonen i filteret 1 ble ventil 11 etter 75 sekunder lukket, og filterkaken 5 tørrblåst 5 minutter med trykkluft 14. Filtratet 18 ble i lamellutskilleren 4 skilt fra trykkluft, som unnvek som avluft 19. Deretter ble ventilen 9 åpnet og den resterende suspensjon trykket fra filteret 1 til skillekaret 5. Etter gjennomslag av trykkluften ble ventilen 11 åpnet, ventil 6 lukket, filteret avspent over ventil 8 og 9 og deretter ble skyveren 10 åpnet. Etter lukking av ventilen 8 ble ved hurtigåpning av ventilen 7 filterkaken 23 kastet av ved hjelp av et pressluftstøt 15. The pressure vessel 2 had a volume of 16 m5. Before the start of filtration, it was 80% filled with suspension 26 by means of pump 3 (transport performance: 12 m> at 8 bar back pressure). At the start of filtration, a flow rate of 10.7 m was set by means of control valve 12 <5> suspension/ hour. The filter 1 was filled from the container 2 within 2 minutes, the suspension being pressed with compressed air 25 at 7 bar through line 27 into the filter 1. The volume flow through line 27 thereby corresponded to 300 m<5>/h. After filling the filter 1 and displacing air from the filter 1, the actual filtering took place immediately. In the course of 90 seconds, 2.9 m<*> of suspension was filtered, corresponding to a volume flow of 116 m'/h through line 27. After a total of 3.5 minutes, valve 12 was closed, valve 6 was opened (feed of compressed air with 7 bar) and the pressure vessel 2 was depressurized by slowly opening the valve 11. When the minimum level of the suspension in the filter 1 was reached, the valve 11 was closed after 75 seconds, and the filter cake 5 was blown dry for 5 minutes with compressed air 14. The filtrate 18 was separated in the lamellar separator 4 from compressed air, which escaped as exhaust air 19. Then the valve 9 was opened and the remaining suspension was pushed from the filter 1 to the separator vessel 5. After the passage of the compressed air, the valve 11 was opened, valve 6 closed, the filter relaxed over valves 8 and 9 and then the pusher 10 opened. After closing the valve 8, by quickly opening the valve 7, the filter cake 23 was thrown off by means of a blast of compressed air 15.
Varigheten av den samlede charge utgjorde 16 minutter. Det fremkom 1,8 t filterkake med 23,4% restfuktighet og 3,2 tonn 655É-ig svovelsyre, tilsvarende 2 m' . Kaketykkkelsen utgjorde ca. 35 mm. The duration of the overall charge was 16 minutes. 1.8 t of filter cake with 23.4% residual moisture and 3.2 tonnes of 655É-ig sulfuric acid were produced, corresponding to 2 m'. The cake thickness was approx. 35 mm.
Claims (7)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19863606986 DE3606986A1 (en) | 1986-03-04 | 1986-03-04 | METHOD FOR SEPARATING SOLIDS FROM SOLID-SUSPENSIONS |
Publications (4)
| Publication Number | Publication Date |
|---|---|
| NO870642D0 NO870642D0 (en) | 1987-02-18 |
| NO870642L NO870642L (en) | 1987-09-07 |
| NO166621B true NO166621B (en) | 1991-05-13 |
| NO166621C NO166621C (en) | 1991-08-21 |
Family
ID=6295429
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO870642A NO166621C (en) | 1986-03-04 | 1987-02-18 | PROCEDURE FOR SEPARATING SOLID SUBSTANCES FROM SOLID SUSPENSIONS. |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP0235689B1 (en) |
| AU (1) | AU585134B2 (en) |
| CA (1) | CA1318257C (en) |
| DE (2) | DE3606986A1 (en) |
| FI (1) | FI89874C (en) |
| NO (1) | NO166621C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3876995D1 (en) | 1988-10-06 | 1993-02-04 | Kronos Titan Gmbh | METHOD AND DEVICE FOR PROCESSING AN IRON (II) SULFATE CONTAINING SULFURIC ACID SOLUTION. |
| NL1023398C2 (en) * | 2003-05-13 | 2004-11-16 | Amafilter Bv | Method and device for filtering an unfiltered residual content in a filter device for liquids. |
| DE102006046214B3 (en) * | 2006-09-29 | 2008-04-30 | Siemens Ag | Fluid collection device |
| DE102010016394A1 (en) * | 2010-04-12 | 2012-05-10 | Solar Und Vakuum Technologie (Svt) A.G. | Solid/liquid mixtures dehumidifying and cleaning method, involves supplying liquid from separating bottom to storage tank, and cooling down heating plates as condensate over drain pipe while providing cleaned vapor |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA981595A (en) * | 1972-06-15 | 1976-01-13 | Dorr-Oliver Incorporated | Defouling ultrafiltration cells |
| DE2831607A1 (en) * | 1978-07-19 | 1980-01-31 | Peter Ueberall | Filter with automatic cleaning action - using air cushion used to backflush element at regular intervals, for use on car wash plants |
| DD159605A1 (en) * | 1981-06-11 | 1983-03-23 | Helmut Hartmann | METHOD AND DEVICE FOR MULTI-STAGE FILTRATION OF PHOTO BAGS |
| JPS58186407A (en) * | 1982-04-12 | 1983-10-31 | アムステツド・インダストリ−ス・インコ−ポレ−テツド | Filter apparatus and method |
| US4469594A (en) * | 1982-11-12 | 1984-09-04 | Harnischfeger Corporation | High pressure hydraulic system and self-cleaning filter assembly therefor |
-
1986
- 1986-03-04 DE DE19863606986 patent/DE3606986A1/en not_active Withdrawn
-
1987
- 1987-02-18 NO NO870642A patent/NO166621C/en unknown
- 1987-02-19 DE DE8787102365T patent/DE3772222D1/en not_active Expired - Lifetime
- 1987-02-19 EP EP87102365A patent/EP0235689B1/en not_active Expired - Lifetime
- 1987-03-02 FI FI870897A patent/FI89874C/en not_active IP Right Cessation
- 1987-03-02 CA CA000530895A patent/CA1318257C/en not_active Expired - Fee Related
- 1987-03-02 AU AU69655/87A patent/AU585134B2/en not_active Ceased
Also Published As
| Publication number | Publication date |
|---|---|
| EP0235689B1 (en) | 1991-08-21 |
| EP0235689A2 (en) | 1987-09-09 |
| DE3606986A1 (en) | 1987-09-10 |
| AU6965587A (en) | 1987-09-10 |
| FI89874B (en) | 1993-08-31 |
| FI870897A (en) | 1987-09-05 |
| NO870642D0 (en) | 1987-02-18 |
| CA1318257C (en) | 1993-05-25 |
| NO166621C (en) | 1991-08-21 |
| DE3772222D1 (en) | 1991-09-26 |
| EP0235689A3 (en) | 1988-11-17 |
| NO870642L (en) | 1987-09-07 |
| AU585134B2 (en) | 1989-06-08 |
| FI89874C (en) | 1993-12-10 |
| FI870897A0 (en) | 1987-03-02 |
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