NO873994L - ROEKGASSLEDNING. - Google Patents
ROEKGASSLEDNING.Info
- Publication number
- NO873994L NO873994L NO873994A NO873994A NO873994L NO 873994 L NO873994 L NO 873994L NO 873994 A NO873994 A NO 873994A NO 873994 A NO873994 A NO 873994A NO 873994 L NO873994 L NO 873994L
- Authority
- NO
- Norway
- Prior art keywords
- catalyst
- flue gas
- gas line
- ammonia
- line according
- Prior art date
Links
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 69
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 66
- 239000003054 catalyst Substances 0.000 claims description 51
- 239000003546 flue gas Substances 0.000 claims description 47
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 34
- 229910021529 ammonia Inorganic materials 0.000 claims description 32
- 239000000463 material Substances 0.000 claims description 18
- 238000007254 oxidation reaction Methods 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 230000003647 oxidation Effects 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 2
- 239000002815 homogeneous catalyst Substances 0.000 claims description 2
- 229910052750 molybdenum Inorganic materials 0.000 claims description 2
- 239000011733 molybdenum Substances 0.000 claims description 2
- 229910021536 Zeolite Inorganic materials 0.000 claims 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims 1
- 239000010457 zeolite Substances 0.000 claims 1
- 235000019391 nitrogen oxide Nutrition 0.000 description 20
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 238000006722 reduction reaction Methods 0.000 description 8
- 229960003753 nitric oxide Drugs 0.000 description 6
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 3
- 229910000476 molybdenum oxide Inorganic materials 0.000 description 3
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- QGLKJKCYBOYXKC-UHFFFAOYSA-N nonaoxidotritungsten Chemical compound O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1 QGLKJKCYBOYXKC-UHFFFAOYSA-N 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- 239000006163 transport media Substances 0.000 description 2
- 229910001930 tungsten oxide Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- XHCLAFWTIXFWPH-UHFFFAOYSA-N [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] XHCLAFWTIXFWPH-UHFFFAOYSA-N 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000009877 rendering Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 229910001935 vanadium oxide Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Catalysts (AREA)
- Chimneys And Flues (AREA)
- Seasonings (AREA)
Description
Oppfinnelsen angår en røkgassledning med en innsprøytningsan-ordning for ammoniakk og med en katalysatoranordning til reduksjon av nitrogenet i nærvær av ammoniakk og oksygen. The invention relates to a flue gas line with an injection device for ammonia and with a catalyst device for reducing the nitrogen in the presence of ammonia and oxygen.
Det er allerede foreslått en anordning til reduksjon av nitrogen i røkgasser (P3627834 .3), hvor det i den til avgass-skorstenen førende røkgassledning etter hverandre er innebygget en første varmeveksler, et røkgassavsvovlingsanlegg, en til den første varmeveksler tilkoblet annen varmeveksler til gjen-oppvarming av de avsvovlede røkgasser, et anlegg til reduksjon av nitrogenoksider i røkgassene og en ytterligere varmeveksler til regenerering av den betydelige varme som finnes i de til skorstenen tilstrømmende denitrogenerte røkgasser. Med denne anordning er en energimessig rasjonell reduksjon av nitrogenoksidene i røkgassene mulig. Graden av reduksjon av nitrogenoksidene som derved oppnås tilsvarer arten av det anvendte denitrogeneringsanlegg, også kalt DENOX-anlegg. A device for reducing nitrogen in flue gases has already been proposed (P3627834 .3), where a first heat exchanger, a flue gas desulphurisation system, a second heat exchanger connected to the first heat exchanger, and another heat exchanger connected to the first heat exchanger are built into the flue gas line leading to the flue gas chimney. heating of the desulphurised flue gases, a plant for reducing nitrogen oxides in the flue gases and a further heat exchanger for regenerating the significant heat contained in the denitrogenised flue gases flowing into the chimney. With this device, an energetically rational reduction of the nitrogen oxides in the flue gases is possible. The degree of reduction of the nitrogen oxides thereby achieved corresponds to the nature of the denitrogenation plant used, also called DENOX plant.
Fra DE-PS 24 58 888 er det allerede kjent en katalysator til reduksjon av nitrogenoksider og som i det vesentlige består av titandioksid, vanadiumpentoksid og ytterligere metall-oksider. Denne katalysator egner seg til å redusere røkgasser i nærvær av ammoniakk og oksygen til nitrogen og vann. Det er imidlertid et særtrekk ved disse og andre katalysatorer til reduksjon av nitrogenoksider i nærvær av ammoniakk at mengden av den i røkgassen gjenværende, ikke omdannede nitrogenoksid - den såkalte rest - utgjør ca. 10% av det opprinnelig fore-kommende nitrogenoksid. Riktignok er det kjent at denne rest kan la seg redusere ytterligere når man arbeider med et overskudd av ammoniakk. I dette tilfelle ville det imidlertid for-bli ikke omdannet ammoniakk i røkgassen. Denne overskuddsammoniakk må i samsvar med gjeldende utslippsforskrifter for røk-gass ikke overskride en meget lav verdi som ligger på 4 mg/Nm"^ . Av disse grunner har det tidligere vært uunngåelig å måtte tolerere en liten rest av ikke omdannede nitrogenoksider i røkgassen. From DE-PS 24 58 888, a catalyst for the reduction of nitrogen oxides is already known which essentially consists of titanium dioxide, vanadium pentoxide and further metal oxides. This catalyst is suitable for reducing flue gases in the presence of ammonia and oxygen to nitrogen and water. However, it is a distinctive feature of these and other catalysts for the reduction of nitrogen oxides in the presence of ammonia that the amount of unconverted nitrogen oxide remaining in the flue gas - the so-called residue - amounts to approx. 10% of the originally occurring nitrogen oxide. Admittedly, it is known that this residue can be further reduced when working with an excess of ammonia. In this case, however, unconverted ammonia would remain in the flue gas. In accordance with current emission regulations for flue gas, this excess ammonia must not exceed a very low value of 4 mg/Nm"^. For these reasons, it has previously been unavoidable to have to tolerate a small residue of unconverted nitrogen oxides in the flue gas.
Oppfinnelsens hensikt er å skaffe en fremgangsmåte med hvilken restinnholdet av nitrogenoksider i røkgassen lar seg redusere ytterligere, uten å få utillatelig høye konsentrasjoner av andre skadelige stoffer i røkgassen. The purpose of the invention is to provide a method by which the residual content of nitrogen oxides in the flue gas can be further reduced, without obtaining unacceptably high concentrations of other harmful substances in the flue gas.
Denne hensikt oppnås ved de trekk som er angitt i krav 1. Ytterligere hensiktsmessige utforminger er vist i kravene 2-9. This purpose is achieved by the features specified in claim 1. Further suitable designs are shown in claims 2-9.
Ved innbygging av henholdsvis et katalysatormateriale til reduksjon av nitrogenoksider og et katalysatormateriale til oksidasjon av ammoniakk skaffes forutsetningen for å sprøyte inn et overskudd av ammoniakk i røkgassene uten at det til slutt gjenværende overskudd av ammoniakk belaster de denitrogenerte røkgassene. Dermed skaffes også forutsetningen for å ytterligere å redusere resten av de ikke omdannede nitrogenoksider. By incorporating, respectively, a catalyst material for the reduction of nitrogen oxides and a catalyst material for the oxidation of ammonia, the prerequisite is provided for injecting an excess of ammonia into the flue gases without the ultimately remaining excess of ammonia burdening the denitrogenized flue gases. This also provides the prerequisite for further reducing the rest of the unconverted nitrogen oxides.
Riktignok er det fra "Journal of Catalysis", 40, 312-317 (1975) og fra "Journal of Catalysis", 37, 258-266 (1975) kjent katalysatorer til oksidasjon av ammoniakk i nærvær av oksygen for fremstilling av nitrogen. Disse undersøkelsene går imidlertid ut fra helt andre problemstillinger, som er uten relevans for røkgassdenitrogenering. Admittedly, from the "Journal of Catalysis", 40, 312-317 (1975) and from the "Journal of Catalysis", 37, 258-266 (1975), catalysts for the oxidation of ammonia in the presence of oxygen to produce nitrogen are known. However, these investigations are based on completely different issues, which are irrelevant to flue gas denitrogenation.
Effektiviteten for røkgassledningen i henhold til oppfinnelsen maksimeres når på fordelaktig måte det første katalysatormateriale er anbragt i en katalysatorblokk, som er innebygget foran det i en annen katalysatorblokk innførte andre katalysatormateriale. Ved reduksjon av nitrogenoksidene står i dette tilfelle fremdeles det uforminskede overskudd av ammoniakk til disposisjon og denne restandel blir først oksidert når nitrogenoksidene i røkgassen er spaltet. The efficiency of the flue gas line according to the invention is maximized when the first catalyst material is advantageously placed in a catalyst block, which is built in front of the second catalyst material introduced in another catalyst block. When the nitrogen oxides are reduced, in this case the undiminished surplus of ammonia is still available and this residual portion is only oxidized when the nitrogen oxides in the flue gas have been decomposed.
En forenklet konstruksjon fås når de to katalysatormaterialene er arbeidet sammen til en enhetlig katalysatormasse slik det er foretatt ved en hensiktsmessig videreutvikling av oppfinnelsen. Dette letter vedlikeholdet og lagerholdet av katalysator-materialet, og utelukker forvekslinger ved vedlikeholds-arbeidene . A simplified construction is obtained when the two catalyst materials are worked together into a uniform catalyst mass, as has been done in an appropriate further development of the invention. This facilitates the maintenance and storage of the catalyst material, and excludes mix-ups during maintenance work.
Fordelaktig kan molybdenoksidandelen økes for å forsterke ammoniakkoksidasjon ved bruk av et reduksjonskatalysator-materiale som består enten av titandioksid, vanadiumpentoksid, molybdenoksid eller wolframoksid. Dette fører til et enhetlig katalysatorlegeme som har en god omdannelseshastighet for nitrogenoksider og er relativt ufølsomt overfor overstøkiomet-riske ammoniakkmengder. Ytterligere trekk ved oppfinnelsen blir forklart i tilknytning til et på tegningen fremstilt utførelses-eksempel. Advantageously, the molybdenum oxide proportion can be increased to enhance ammonia oxidation by using a reduction catalyst material consisting of either titanium dioxide, vanadium pentoxide, molybdenum oxide or tungsten oxide. This leads to a uniform catalyst body which has a good conversion rate for nitrogen oxides and is relatively insensitive to over-stoichiometric amounts of ammonia. Further features of the invention are explained in connection with an embodiment shown in the drawing.
- Fig. 1 viser en skjematisk gjengivelse av en røkgassledning som er utført i henhold til oppfinnelsen og fører til en - Fig. 1 shows a schematic rendering of a flue gas line which is made according to the invention and leads to a
skorsten.the chimney.
- Fig. 2 viser en forstørret oversikt over et DENOX-anlegg- Fig. 2 shows an enlarged view of a DENOX plant
i henhold til oppfinnelsen.according to the invention.
På fig. 1 betegner 1 et passende forbrenningsanlegg hvis røk-gassledning 2 fører til en skorsten 3. I røkgassledningen 2 In fig. 1 denotes 1 a suitable combustion plant whose flue gas line 2 leads to a chimney 3. In the flue gas line 2
er det i strømningsretningen etter hverandre innbygget en første varmeveksler 4, et røkgassav.svovlingsanlegg 5, en annen varmeveksler 6, en ammoniakkinnsprøytningsanordning 7, et DENOX--anlegg 8 og en tredje varmeveksler 9. Den første og den annen varmeveksler er på sekundærsiden forbundet med hverandre over rørledninger 10, 11 for varmetransportmedier. I DENOX-anlegget er to katalysatorblokk'er 12, 13 koblet etter hverandre i strøm-ningsretningen for røkgassen. Den første katalysatorblokk 12 inneholder et katalysatormateriale til reduksjon av nitrogenoksider i nærvær av ammoniakk. Den annen katalysatorblokk 13 inneholder et katalysatormateriale til oksidasjon av ammoniakk i nærvær av oksygen. a first heat exchanger 4, a flue gas desulphurisation system 5, a second heat exchanger 6, an ammonia injection device 7, a DENOX system 8 and a third heat exchanger 9 are built in in succession in the flow direction. The first and second heat exchangers are connected on the secondary side with each other over pipelines 10, 11 for heat transport media. In the DENOX plant, two catalyst blocks 12, 13 are connected one behind the other in the direction of flow of the flue gas. The first catalyst block 12 contains a catalyst material for the reduction of nitrogen oxides in the presence of ammonia. The second catalyst block 13 contains a catalyst material for the oxidation of ammonia in the presence of oxygen.
Ved drift av forbrenningsanlegget 1 dannes varme røkgasserDuring operation of the combustion plant 1, hot flue gases are formed
som ved siden av støv, aske og andre gassformede bestanddeler også inneholder overskuddsmengder av oksygen. Disse røkgasser strømmer på sin vei til skorstenen 3 først inn i den i røkgass-ledningen 2 innkoblede første varmeveksler 4 og når etter at de der er blitt avkjølet til ca. 160°C, til røkgassavsvovlings- which, in addition to dust, ash and other gaseous components, also contain excess amounts of oxygen. These flue gases flow on their way to the chimney 3 first into the first heat exchanger 4 connected to the flue gas line 2 and when they have cooled to approx. 160°C, for flue gas desulphurisation
anlegget 5. Der blir de på kjent måte befridd for støv og aske-partikler samt for svovelholdige forbindelser. De forlater røkgassavsvovlingsanlegget 5 med ca. 65°C og blir igjen opp-varmet i den etterkoblede andre varmeveksler med den tidligere i første varmeveksler uttatte og til varmetransportmediet over-førte varme til den til DENOX-anleggets katalysator 12, 13 tilpassede optimale gasstemperatur - i foreliggende tilfelle ca. 300°C. facility 5. There, they are freed from dust and ash particles as well as sulfur-containing compounds in a known manner. They leave the flue gas desulphurisation plant 5 with approx. 65°C and is heated again in the downstream second heat exchanger with the heat previously extracted from the first heat exchanger and transferred to the heat transport medium to the optimal gas temperature adapted to the DENOX plant's catalyst 12, 13 - in the present case approx. 300°C.
I de således oppvarmede røkgasser tilføres ammoniakk via inn-sprøytningsanordningen 7. Innsprøytningsmengden blir derved fortrinnsvis justert slik at det i forhold til nødvendige støk-kiometrisk mengde av ammoniakk skaffes et overskudd på 10%. In the flue gases thus heated, ammonia is supplied via the injection device 7. The injection amount is thereby preferably adjusted so that in relation to the required stoichiometric amount of ammonia, an excess of 10% is obtained.
Ved denne overstøkiometriske ammoniakkinnblanding blir effektiviteten av den katalytiske reduksjon av nitrogenoksiden i den første katalysatorblokk 12 tydelig forbedret ovenfor den ellers forventede effektivitet, dvs. at den gjenværende nitrogenoksid-andel reduseres ytterligere. I de mest denitrogerte røkgasser som forlater den første katalysatorblokk 12 befinner det seg imidlertid må pga. av den overstøkiometriske innsprøyting av ammoniakk en merkbar restandel av ikke omdannet ammoniakk. Denne overskuddsammoniakk blir-, nå tilført den annen katalysatorblokk 13 med den i røkgasse.n gjenværende oksygenandel. Da denne katalysatorblokk omfatter'en i og for seg tidligere kjent oksi-das jonskatalysator, blir i denne ammoniakken oksidert med oksygen til nitrogen og vann i henhold til formelen With this over-stoichiometric ammonia mixture, the efficiency of the catalytic reduction of the nitrogen oxide in the first catalyst block 12 is clearly improved above the otherwise expected efficiency, i.e. that the remaining nitrogen oxide proportion is further reduced. However, in the most denitrogenized flue gases leaving the first catalyst block 12 there must be of the over-stoichiometric injection of ammonia a noticeable residual proportion of unconverted ammonia. This excess ammonia is now supplied to the second catalyst block 13 with the remaining proportion of oxygen in the flue gas. As this catalyst block includes the per se previously known oxidation ion catalyst, in this the ammonia is oxidized with oxygen to nitrogen and water according to the formula
4 NH3+ 3022 N2+ 6 H20 4 NH3+ 3022 N2+ 6 H2O
Slike tidligere kjente NH^-oksidasjonskatalysatorer er f.eks. WO^-blandingskatalysatorer. Such previously known NH 3 -oxidation catalysts are e.g. WO^ mixture catalysts.
De varme, avsvovlede og denitrogenerte røkgasser som forlater katalysatoranordningen i DENOX-anlegget 8 blir avkjølt i den etterkoblede tredje varmeveksler 9 til skorstensinngangstempe-raturen på 100°C og unnslipper deretter gjennom skorstenen 2. Ved denne konstruksjon lar den i røkgassen gjenværende ammo-niakkandel seg redusere til under 4 mg/Nm 3 til tross for den overstøkiometriske innsprøyting. Den gjenværende nitrogen_oksid- andel ligger nettopp pga. den overstøkiometriske ammoniakkinn-sprøytning klart under de ellers vanlige 10% av de opprinnelige nitrogenoksider. The hot, desulphurised and denitrogenised flue gases leaving the catalyst device in the DENOX plant 8 are cooled in the downstream third heat exchanger 9 to the chimney entrance temperature of 100°C and then escape through the chimney 2. With this construction, the ammonia remaining in the flue gas allows reduce to below 4 mg/Nm 3 despite the over-stoichiometric injection. The remaining nitrogen_oxide share lies precisely because the over-stoichiometric ammonia injection clearly below the otherwise usual 10% of the original nitrogen oxides.
Det ville også være mulig å sammensmelte de to katalysatorblok-ker som valgfritt kan bestå av korn, lag av fortrinnsvis ku-biske katalysatorStener eller også av plater belagt med katalysatormasse, til en eneste blokk. Det ville også være mulig å forarbeide de to katalysatormaterialene til et eneste homogent blandet katalysatormateriale. I det siste har den prak-tiske fordel at det ved vedlikehold og komplettering kan gås ut fra et homogent materiale. Et slikt homogent katalysatormateriale kunne også dannes ut ifra en kjent katalysator til reduksjon av nitrogenoksidet i nærvær av ammoniakk på basis av titanoksid + vanadiumoksid + molybdenoksid + wolframoksid ved forhøyning av molybdenandelen. It would also be possible to fuse the two catalyst blocks, which can optionally consist of grains, layers of preferably cubic catalyst stones or also of plates coated with catalyst mass, into a single block. It would also be possible to process the two catalyst materials into a single homogeneous mixed catalyst material. In the latter, it has the practical advantage that maintenance and completion can be based on a homogeneous material. Such a homogeneous catalyst material could also be formed from a known catalyst for the reduction of nitrogen oxide in the presence of ammonia on the basis of titanium oxide + vanadium oxide + molybdenum oxide + tungsten oxide by increasing the molybdenum proportion.
Claims (9)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE3632595 | 1986-09-25 |
Publications (2)
Publication Number | Publication Date |
---|---|
NO873994D0 NO873994D0 (en) | 1987-09-24 |
NO873994L true NO873994L (en) | 1988-03-28 |
Family
ID=6310334
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
NO873994A NO873994L (en) | 1986-09-25 | 1987-09-24 | ROEKGASSLEDNING. |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP0261610A1 (en) |
JP (1) | JPS6387521A (en) |
DD (1) | DD264274B5 (en) |
DK (1) | DK174013B1 (en) |
FI (1) | FI88363C (en) |
NO (1) | NO873994L (en) |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DK166377C (en) * | 1989-02-10 | 1993-09-27 | Haldor Topsoe As | PROCEDURE FOR THE REMOVAL OF NITROGEN OXIDES FROM EXHAUST GAS FROM TURBINES |
DE4204603C2 (en) * | 1992-02-15 | 1996-02-29 | Hager & Elsaesser | Device for the multi-stage, catalytic combustion of nitrogenous gases |
JP3349182B2 (en) * | 1992-12-21 | 2002-11-20 | 三菱重工業株式会社 | Ammonia treatment method |
CA2154500C (en) * | 1994-07-28 | 2001-10-02 | Kouzo Iida | Methods of denitrating exhaust gases |
US5770163A (en) * | 1994-12-21 | 1998-06-23 | Mitsubishi Jukogyo Kabushiki Kaisha | System for the recovery of ammonia escaping from an ammonia reduction denitrator |
JP2000093749A (en) | 1998-09-25 | 2000-04-04 | Mitsubishi Heavy Ind Ltd | Gas denitration process |
US6685897B1 (en) | 2000-01-06 | 2004-02-03 | The Regents Of The University Of California | Highly-basic large-pore zeolite catalysts for NOx reduction at low temperatures |
KR20220160765A (en) * | 2021-05-28 | 2022-12-06 | (주)트리플코어스코리아 | NOx Reduction System |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1586530A (en) * | 1977-05-31 | 1981-03-18 | Caterpillar Tractor Co | Two-stage catalysts of engine exhaust |
US4571329A (en) * | 1984-08-13 | 1986-02-18 | Babcock-Hitachi Kabushiki Kaisha | Ammonia reduction-denitration process and apparatus therefor |
-
1987
- 1987-09-08 FI FI873876A patent/FI88363C/en not_active IP Right Cessation
- 1987-09-18 EP EP87113717A patent/EP0261610A1/en not_active Withdrawn
- 1987-09-18 DD DD30705487A patent/DD264274B5/en not_active IP Right Cessation
- 1987-09-21 JP JP62238602A patent/JPS6387521A/en active Pending
- 1987-09-23 DK DK198704988A patent/DK174013B1/en not_active IP Right Cessation
- 1987-09-24 NO NO873994A patent/NO873994L/en unknown
Also Published As
Publication number | Publication date |
---|---|
JPS6387521A (en) | 1988-04-18 |
DK174013B1 (en) | 2002-04-15 |
DD264274B5 (en) | 1996-08-08 |
DK498887D0 (en) | 1987-09-23 |
NO873994D0 (en) | 1987-09-24 |
EP0261610A1 (en) | 1988-03-30 |
FI873876A (en) | 1988-03-26 |
FI873876A0 (en) | 1987-09-08 |
DD264274A1 (en) | 1989-01-25 |
DK498887A (en) | 1988-03-26 |
FI88363B (en) | 1993-01-29 |
FI88363C (en) | 1993-05-10 |
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