NO834785L - PROCEDURE FOR SEPARATION OF VACUUM Suspended Catalyst Particles - Google Patents
PROCEDURE FOR SEPARATION OF VACUUM Suspended Catalyst ParticlesInfo
- Publication number
- NO834785L NO834785L NO834785A NO834785A NO834785L NO 834785 L NO834785 L NO 834785L NO 834785 A NO834785 A NO 834785A NO 834785 A NO834785 A NO 834785A NO 834785 L NO834785 L NO 834785L
- Authority
- NO
- Norway
- Prior art keywords
- liquid
- filter
- filters
- backwashing
- flow
- Prior art date
Links
- 239000002245 particle Substances 0.000 title claims description 16
- 238000000034 method Methods 0.000 title claims description 15
- 238000000926 separation method Methods 0.000 title claims description 5
- 239000003054 catalyst Substances 0.000 title description 15
- 239000007788 liquid Substances 0.000 claims description 32
- 239000000706 filtrate Substances 0.000 claims description 19
- 238000011001 backwashing Methods 0.000 claims description 12
- 238000005984 hydrogenation reaction Methods 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 10
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 8
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- 150000004056 anthraquinones Chemical class 0.000 claims description 7
- 239000007868 Raney catalyst Substances 0.000 claims description 4
- NPXOKRUENSOPAO-UHFFFAOYSA-N Raney nickel Chemical compound [Al].[Ni] NPXOKRUENSOPAO-UHFFFAOYSA-N 0.000 claims description 4
- 229910000564 Raney nickel Inorganic materials 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 230000000717 retained effect Effects 0.000 claims description 4
- 238000001311 chemical methods and process Methods 0.000 claims description 2
- 239000007795 chemical reaction product Substances 0.000 claims description 2
- 230000000737 periodic effect Effects 0.000 claims description 2
- 239000011248 coating agent Substances 0.000 description 7
- 238000000576 coating method Methods 0.000 description 7
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- 230000035699 permeability Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- -1 alkyl anthraquinone Chemical class 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 229910010293 ceramic material Inorganic materials 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000026030 halogenation Effects 0.000 description 1
- 238000005658 halogenation reaction Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000010327 methods by industry Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D37/00—Processes of filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D37/00—Processes of filtration
- B01D37/04—Controlling the filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J25/00—Catalysts of the Raney type
- B01J25/04—Regeneration or reactivation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/48—Liquid treating or treating in liquid phase, e.g. dissolved or suspended
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Description
Denne oppfinnelse angår en fremgangsmåte ved fraskillelseThis invention relates to a method for separation
av i væske suspenderte faste katalysatorpartikler.of solid catalyst particles suspended in liquid.
Innenfor prosessteknikken er det vanlig å utføre reaksjoner mellom gass og væske eller et eller flere i væske oppløste stoffer ved hjelp av i væsker tilstedeværende katalytisk virksomme faste stoffer. Eksempler på slike reaksjoner er hydrogenering, oksydering og halogenering. Katalysatoren kan ha form av et fast sjikt, gjennom hvilket væsken passerer, eller være en sus-pensjon av partikler som gjennom energitilførsel holdes fritt svevende i væsken. Suspensjonskatalysatoren har visse fordeler. Den kan f.eks. suksessivt fornyes ved kontinuerlige prosesser. Within process engineering, it is common to carry out reactions between gas and liquid or one or more substances dissolved in liquid with the help of catalytically active solids present in liquids. Examples of such reactions are hydrogenation, oxidation and halogenation. The catalyst can take the form of a solid layer, through which the liquid passes, or be a suspension of particles that are kept freely floating in the liquid through the supply of energy. The suspension catalyst has certain advantages. It can e.g. successively renewed by continuous processes.
Den dispergerte katalysator bibeholder i flere tilfeller sin aktivitet i betydelige tidsrom, og hvis reaksjonen skal for- In several cases, the dispersed catalyst retains its activity for considerable periods of time, and if the reaction is to
løpe kontinuerlig må katalysatoren derfor holdes tilbake i eller stadig returneres til det reaksjonsrom gjennom hvilket væsken passerer. Dette kan oppnåes ved at den ferdig reagerte væske uttas gjennom et filter som holder katalysatorpartiklene tilbake. run continuously, the catalyst must therefore be retained in or constantly returned to the reaction space through which the liquid passes. This can be achieved by withdrawing the fully reacted liquid through a filter that retains the catalyst particles.
I alminnelighet er den momentane filtratstrømning gjennomIn general, the instantaneous filtrate flow through
et filter direkte proporsjonal med filteroverflaten og trykkfal-• let over samme, samt omvendt proporsjonal med væskens viskositet, samlet mengde belegg på filteroverflaten samt en konstant som er avhengig av beleggets permeabilitet. a filter directly proportional to the filter surface and the pressure drop over the same, as well as inversely proportional to the viscosity of the liquid, the total amount of coating on the filter surface and a constant that depends on the permeability of the coating.
Det er kjent at en filteroverflate momentant kan befriesIt is known that a filter surface can be momentarily freed
for overflatebelegget gjennom såkalt tilbakespyling, som inne-bærer at væske presses gjennom filteret i motsatt retning mot den normale filtratstrømning. I US-patent 2.990.238 beskrives tilbakespyling ved hjelp av en stempel- eller membranpumpe som i den ene slagretning suger ut filtrat og i den andre trykker tilbake en del av filtratet gjennom filteret. for the surface coating through so-called backwashing, which involves liquid being pushed through the filter in the opposite direction to the normal filtrate flow. In US patent 2,990,238, backwashing is described using a piston or diaphragm pump which sucks out filtrate in one direction of stroke and pushes back part of the filtrate through the filter in the other.
Som vist på fig. 1 i det nevnte patent anvendes bare halv-parten av den tilgjengelige tid for uttak av filtrat uansett pumpeslagfrekvensen, som angies å være 1 - 500 pr. min. Dessuten angies det at tilbakestrømningen bør være 20 - 70% av den ut-sugede filtratmengde, hvilket ytterligere minsker produktstrøm-ningen i tilsvarende grad. I henhold til denne fremgangsmåte kan tilbakespylingsstrømningen ikke bli større enn filtratstrøm-ningen. As shown in fig. 1 in the aforementioned patent, only half of the available time is used for withdrawing filtrate regardless of the pump stroke frequency, which is stated to be 1 - 500 per my. In addition, it is stated that the return flow should be 20 - 70% of the extracted filtrate quantity, which further reduces the product flow to a corresponding degree. According to this method, the backwash flow cannot be greater than the filtrate flow.
I BRD-patent 1.542.089 vises et filterarrangement ved kontinuerlig hydrogenering. Filtratet passerer ut gjennom en stillestående sentrifugalpumpe. Når pumpen startes, trykker den filtrat tilbake gjennom filteret. Hydrogeneringen utføres ved sirkulasjon av væske og i væsken dispergert hydrogengass, hvorved ifølge eksempel 1 strømningshastigheten er 0j7 - 2,8 m/s. Filteret er plassert ved siden av sirkulasjonsstrømmen, hvorfor strømningshastigheten under filtreringen går mot null ved filterets øverste del. I beskrivelsen angies at tilbakespyling kan skje i løpet av noen sekunder. Konsentrasjonen av faste partikler angies i eksemplene å være 1 - 5 g/l. BRD patent 1,542,089 shows a filter arrangement for continuous hydrogenation. The filtrate passes out through a stationary centrifugal pump. When the pump is started, it pushes the filtrate back through the filter. The hydrogenation is carried out by circulation of liquid and hydrogen gas dispersed in the liquid, whereby according to example 1 the flow rate is 0j7 - 2.8 m/s. The filter is placed next to the circulation flow, which is why the flow rate during filtration goes towards zero at the top of the filter. The description states that backwashing can take place within a few seconds. The concentration of solid particles is stated in the examples to be 1 - 5 g/l.
I Britisk patent 959.583 beskrives hydrogenering av enBritish patent 959,583 describes the hydrogenation of a
væske bestående av alkylantrakinon oppløst i organiske løsnings-midler. Denne hydrogenering er en delprosess i den kjente antrakinonprosessen for fremstilling av hydrogenperoksyd. Den i opp-løsningen suspenderte hydrogeneringskatalysator holdes tilbake på et filter som periodisk tilbakespyles ved hjelp av en pumpe. Ytterligere opplysninger angående tilbakespylingen og katalysatoren savnes. liquid consisting of alkyl anthraquinone dissolved in organic solvents. This hydrogenation is a partial process in the known anthraquinone process for the production of hydrogen peroxide. The hydrogenation catalyst suspended in the solution is retained on a filter which is periodically backwashed using a pump. Further information regarding the backwash and the catalyst is missing.
I BRD-patent 1.272.292 eksemplifiseres samme hydrogenerings-prosess. Som filtermedium anvendes et porøst fast karbonmateri-ale. Antrakinonoppløsningen inneholder som katalysator 0,07 BRD patent 1,272,292 exemplifies the same hydrogenation process. A porous solid carbon material is used as filter medium. The anthraquinone solution contains 0.07 as catalyst
vekt% palladiumsvart. Katalysatorens kornstørrelse er 0,01 -wt% palladium black. The catalyst grain size is 0.01 -
3 2 1 ym. Filtratstrømningen er 0,46 m pr. time og m filteroverflate. I beskrivelsen angies at karbonfilteret skal tilbakespyles 3 - 10 s med 20 - 30 min. mellomrom. 3 2 1 etc. The filtrate flow is 0.46 m per hour and m filter surface. The description states that the carbon filter must be backwashed for 3 - 10 s with 20 - 30 min. space.
Ved den i antrakinonprosessen inngående hydrogenering anvendes foruten palladiumsvart også Raney-nikkel eller eksempelvis palladium anbragt på en såkalt bærer, vanligvis et keramisk materiale. Disse suspensjonskatalysatorer anvendes i høyere konsentrasjon enn 5 g pr. 1 væske og partikkelstørrelsen er gjennomsnittlig større enn 1 ym. In the hydrogenation included in the anthraquinone process, in addition to palladium black, Raney nickel or, for example, palladium placed on a so-called carrier, usually a ceramic material, is used. These suspension catalysts are used in a higher concentration than 5 g per 1 liquid and the particle size is on average larger than 1 um.
Ved anvendelse av slike katalysatorer har uttak av produkt-væske gjennom filter vært forenet med så store vanskeligheter at katalysatorfraskillelsen i visse tilfeller ble utført ved hjelp av hydrosyklon og/eller sentrifuge. When using such catalysts, extracting the product liquid through a filter has been associated with such great difficulties that the catalyst separation was in certain cases carried out with the aid of a hydrocyclone and/or centrifuge.
Ved den foreliggende oppfinnelse tilveiebringes en fremgangsmåte ved fraskillelse av i væske suspenderte faste partikler, så som Raney-nikkel, som er katalytisk virksomme ved kontinuerlige kjemiske prosesser, så som hydrogeneringsprosessen som inngår i antrakinonprosessen ved fremstilling av hydrogenperoksyd, og hvilke partiklers kornstørrelse til mer enn 75% er større enn 1 ym, samt hvilke foreligger i en konsentrasjon som holdes høyere enn gjennomsnittlig 5 g pr. 1 væske, hvorved væsken med reaksjonsprodukt etter passasje av et reaksjonsrom bringes til å passere gjennom et eller flere filtere, og de faste partikler som herved holdes tilbake på filteroverflaten, løsgjøres ved periodisk tilbakespyling og deretter på ny suspenderes i reaksjonsrommet, hvilken fremgangsmåte erkarakterisert vedat tilbakespylingen utføres med en væskemengde som er større enn den væskemengde som kan innesluttes i filteret eller filtrene, og ved at den spesifike tilbakespylingsstrømning gjennom filteret eller filtrene avpasses slik at den blir større enn den spesifike filtratstrøm-ning gjennom filteret eller filtrene i de første 20 s etter tilbakespyling . The present invention provides a method for the separation of solid particles suspended in a liquid, such as Raney nickel, which are catalytically active in continuous chemical processes, such as the hydrogenation process which is part of the anthraquinone process in the production of hydrogen peroxide, and which particles have a grain size of more than 75% are larger than 1 ym, as well as which are present in a concentration that is kept higher than the average 5 g per 1 liquid, whereby the liquid with reaction product after passing through a reaction chamber is made to pass through one or more filters, and the solid particles that are thereby retained on the filter surface are loosened by periodic backwashing and then resuspended in the reaction chamber, which method is characterized by the backwashing is carried out with a quantity of liquid that is greater than the quantity of liquid that can be contained in the filter or filters, and by adjusting the specific backwash flow through the filter or filters so that it becomes greater than the specific filtrate flow through the filter or filters in the first 20 s after backwash .
Ved hjelp av den foreliggende fremgangsmåte er det mulig, under langvarige kontinuerlige forhold, å oppnå en effektiv 3 2 spesifik filtratmengde som er større enn 0,5 m pr. time og m filteroverflate selv når katalysatorkonsentrasjonen er større enn 5 g pr. 1 væske og/eller belegningen på filteret har en lav permeabilitet. With the help of the present method, it is possible, under long-term continuous conditions, to achieve an effective 3 2 specific filtrate amount which is greater than 0.5 m per hour and m filter surface even when the catalyst concentration is greater than 5 g per 1 liquid and/or the coating on the filter has a low permeability.
Belegget/belegningen på filteret er ikke bare en obstruksjon. Den tjener også som et filter som fanger opp de partikler som ellers hadde kunnet passere gjennom porene i det faste filter. Ved hver tilbakespyling frilegges filteroverflaten for sådan penetrering. Med hensyn hertil og med hensyn til optimalt uttak av produktstrømning har det vist seg mest hensiktsmessig å til-bakespyle med tidsmellomrom fra en tredjedels minutt til 20 min. avhengig av konsentrasjonen av faste partikler i væsken og be-legningens permeabilitet. The coating on the filter is not just an obstruction. It also serves as a filter that captures the particles that could otherwise pass through the pores of the fixed filter. With each backwash, the filter surface is exposed for such penetration. With regard to this and with regard to optimal withdrawal of product flow, it has proven most appropriate to backwash with time intervals from one-third of a minute to 20 minutes. depending on the concentration of solid particles in the liquid and the permeability of the coating.
Tilbakespylingen skal ikke bare skylle bort den ytre beleg-ning på filteroverflaten, men også om mulig spyle tilbake de partikler som har trengt inn i filtermediets poresystem. The backwash should not only wash away the outer coating on the filter surface, but also, if possible, wash back the particles that have penetrated the filter medium's pore system.
For å oppnå dette skal tilbakespylingen i henhold til oppfinnelsen utføres med en væskemengde som er større enn den som innesluttes i filtermediet og fortrinnsvis 2-10 ganger større enn denne mengde. Dessuten skal den spesifike tilbakespylings-strømning være større enn den spesifike filtratstrømning i de første 20 sekunder etter en tilbakespyling. Det har også vist seg å være fordelaktig at væsken ved de overflater av filteret eller filtrene som vender mot reaksjonsrommet, bibringes en bevegelse i nærheten av filteroverflåtene som gjennomsnittlig er større enn 0,1 m/s. In order to achieve this, the backwashing according to the invention must be carried out with a quantity of liquid which is greater than that contained in the filter medium and preferably 2-10 times greater than this quantity. Moreover, the specific backwash flow must be greater than the specific filtrate flow in the first 20 seconds after a backwash. It has also been shown to be advantageous that the liquid at the surfaces of the filter or filters facing the reaction chamber is imparted a movement in the vicinity of the filter surfaces which is on average greater than 0.1 m/s.
Katalysatorpartiklenes kornstørrelse er fortrinnsvis forThe grain size of the catalyst particles is preferably too
mer enn 75%'s vedkommende større enn 1 ym.more than 75% of them larger than 1 ym.
Oppfinnelsen belyses nærmere ved hjelp av nedenstående eksempler og tegningen. The invention is explained in more detail with the help of the below examples and the drawing.
Eksempel 1 (sammenligningseksempel)Example 1 (comparison example)
På fig. 1 vises filtreringsforløpet ved hydrogenering av antrakinonderivater oppløst i organiske løsningsmidler. Løsnin-gen inneholder 110 g/l suspendert Raney-nikkel med kornstørrelse. fra ca. 1 ym opp til 0,5 mm, hvorved mer enn 75% var større enn 1 ym. Filtermediet var oppbygget av sintrede partikler av syre-fast stål. Godstykkelsen var 2 mm og porøsiteten var ca. 40%. In fig. 1 shows the filtration process by hydrogenation of anthraquinone derivatives dissolved in organic solvents. The solution contains 110 g/l of suspended Raney nickel with grain size. from approx. 1 ym up to 0.5 mm, whereby more than 75% were larger than 1 ym. The filter medium was made up of sintered particles of acid-resistant steel. The material thickness was 2 mm and the porosity was approx. 40%.
Den maksimale porevidde var 8 ym.The maximum pore width was 8 ym.
Før filtreringsforsøket var filtermediets porsystem blitt renset ved kjemisk behandling. Ved anvendelse av mekanisk energi ble oppløsningen ved filteroverflaten gitt en turbulent strømnings-hastighet som gjennomsnittlig var større enn 0,1 m/s. Tilbakespyling ble utført i 6 s, og filtratstrømningen var da avstengt i tilsammen 12 s. Tilbakespylingen ble utført med 10 min. mellomrom. Before the filtration test, the pore system of the filter medium had been cleaned by chemical treatment. When mechanical energy was applied, the solution at the filter surface was given a turbulent flow velocity which was on average greater than 0.1 m/s. Backwashing was carried out for 6 s, and the filtrate flow was then shut off for a total of 12 s. The backwashing was carried out for 10 min. space.
Etter fradrag for den gjennom filteret tilbakespylte hydro-generte oppløsning var den gjennomsnittlige filtratstrømning i hver 10 min. periode ca. 1,3 m 3 pr. m 2 filteroverflate og time. Etter ti døgns kontinuerlig drift var den effektive filtratstrøm-ning mindre enn 1,0 m 3 /m 2. Hydrogeneringen inngikk i antrakinonprosessen for fremstilling av hydrogenperoksyd. After deduction for the hydrogenated solution flushed back through the filter, the average filtrate flow in every 10 min. period approx. 1.3 m 3 per m 2 filter surface and hour. After ten days of continuous operation, the effective filtrate flow was less than 1.0 m 3 /m 2. The hydrogenation was included in the anthraquinone process for the production of hydrogen peroxide.
Eksempel 2Example 2
På fig. 2 vises filtreringsforløpet ved samme forutsetninger som i eksempel 1. Tilbakespylingen ble utført i 2 s hvert min. Den gjennomsnittlige effektive filtratstrømning var 2,25 m 3 /m 2 It. Etter 60 døgns kontinuerlig drift var den effektive filtrat-strømning ca. 2,1 m^/m2/t.In fig. 2 shows the filtration process under the same conditions as in example 1. The backwashing was carried out for 2 s every min. The average effective filtrate flow was 2.25 m 3 /m 2 It. After 60 days of continuous operation, the effective filtrate flow was approx. 2.1 m^/m2/h.
Claims (3)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE8207376A SE8207376L (en) | 1982-12-23 | 1982-12-23 | PROCEDURE FOR SEPARATION OF VETERINARY SUSPENDED CATALYST PARTICLES |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NO834785L true NO834785L (en) | 1984-06-25 |
Family
ID=20349129
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO834785A NO834785L (en) | 1982-12-23 | 1983-12-22 | PROCEDURE FOR SEPARATION OF VACUUM Suspended Catalyst Particles |
Country Status (3)
| Country | Link |
|---|---|
| CA (1) | CA1208619A (en) |
| NO (1) | NO834785L (en) |
| SE (1) | SE8207376L (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4217245A1 (en) * | 1992-05-25 | 1993-12-02 | Degussa | Process for the separation of catalyst-free working solution from the hydrogenation of the Anthrachionverfahrens for the production of hydrogen peroxide |
| DE4418931C2 (en) * | 1994-05-31 | 1997-06-19 | Degussa | Process for separating catalyst-free working solution from the hydrogenation cycle of the anthraquinone process for the production of hydrogen peroxide |
-
1982
- 1982-12-23 SE SE8207376A patent/SE8207376L/en not_active Application Discontinuation
-
1983
- 1983-12-20 CA CA000443852A patent/CA1208619A/en not_active Expired
- 1983-12-22 NO NO834785A patent/NO834785L/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| SE8207376D0 (en) | 1982-12-23 |
| SE8207376L (en) | 1984-06-24 |
| CA1208619A (en) | 1986-07-29 |
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