SI9520141A - Method for separating gaseous pollutants from hot process gases - Google Patents
Method for separating gaseous pollutants from hot process gases Download PDFInfo
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- SI9520141A SI9520141A SI9520141A SI9520141A SI9520141A SI 9520141 A SI9520141 A SI 9520141A SI 9520141 A SI9520141 A SI 9520141A SI 9520141 A SI9520141 A SI 9520141A SI 9520141 A SI9520141 A SI 9520141A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
-
- 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
- B01D53/81—Solid phase processes
Abstract
Description
ABB FLAKT AB Nacka, ŠvedskaABB FLAKT AB Nacka, Sweden
Postopek ločevanja plinskih onesnaževalcev od vročih procesnih plinovThe process of separating gas pollutants from hot process gases
Predloženi izum se nanaša na postopek ločevanja plinskih onesnaževalcev, kot je žveplov dioksid, od vročih procesnih plinov, kot so dimni plini, pri katerem (postopku) procesni plini potujejo skozi kontaktni reaktor, v katerem se vpojno gradivo v obliki delcev, ki reagira s plinskimi onesnaževalci, uvaja v navlaženem stanju v procesne pline za pretvarjanje plinskih onesnaževalcev v ločljiv prah, nakar procesni plini potujejo skozi separator za prah, v katerem se prah loči od procesnih plinov in od katerega iztekajo očiščeni procesni plini, pri čemer del prahu, ločenega v separatorju za prah, potuje v mešalnik, kjer se zmeša in dopolni z vodo, da se navlaži, nakar se recirkulira kot vpojno gradivo, s tem ko se uvaja v procesne pline skupaj z dodatkom svežega vpojnega gradiva.The present invention relates to a process for separating gas pollutants such as sulfur dioxide from hot process gases, such as flue gases, in which process gases are passed through a contact reactor in which absorbent particulate material reacts with gas contaminants, introduces, in a moistened state, process gases to convert gas contaminants into separable dust, after which the process gases pass through a dust separator in which the dust is separated from the process gases and from which the purified process gases flow, with part of the dust separated in the separator for dust, it travels to a mixer, where it is mixed and filled with water to moisten, then recirculated as absorbent material, being introduced into process gases with the addition of fresh absorbent material.
Zgoraj opisani postopek ločevanja plinskih onesnaževalcev od vročih plinov je znan npr. iz SE 8504675-3 in SE 8904106-5. Po teh dveh dokumentih se prednostno uporablja gašeno apno (kalcijev hidroksid) v obliki kot delci kot sveže vpojno gradivo. To vpojno gradivo se zmeša s prahom, ki se je ločil od procesnih plinov v separatorju za prah, nakar se v zmes doda vodo in se jo v tako navlaženem stanju uvaja v dimne pline v kontaktnem reaktorju. Gašeno apno je sorazmerno drago, pa so zato izvedli razne poskuse, da bi namesto njega uporabljali žgano apno (kalcijev oksid), ki je opazno cenejše. V teh poskusih so morali uporabiti postrojenje, v katerem so najprej morali žgano apno ugasiti, t.j. kalcijevemu oksidu je bila dana možnost reagirati z vodo. daje nastal kalcijev hidroksid, preden so ga uvedli v čistilni proces. Tovrstno postrojenje za gašenje apna je drago, kar pomeni, da pri zamenjavi gašenega apna z žganim apnom ni pričakovati dobička.The procedure described above for separating gas pollutants from hot gases is known e.g. from SE 8504675-3 and SE 8904106-5. According to these two documents, slaked lime (calcium hydroxide) in the form of particles as fresh absorbent material is preferably used. This absorbent material is mixed with the dust which has separated from the process gases in the dust separator, and then water is added to the mixture and introduced into the flue gas in the contact reactor in such a moistened state. Extinguished lime is relatively expensive, so various experiments have been carried out to use calcined lime (calcium oxide), which is noticeably cheaper. In these experiments, they had to use a plant where they first had to quench the calcined lime, i.e. calcium oxide was given the opportunity to react with water. it produces calcium hydroxide before it is introduced into the purification process. This kind of lime quenching plant is expensive, which means that no profit is expected when replacing slaked lime with calcined lime.
Cilj pričujočega izuma je ustvariti postopek ločevanja plinskih onesnaževalcev od vročih procesnih plinov, v katerem gašeno apno lahko zamenjamo z žganim apnom, ne da bi rabili drago, posebno postrojenje za gašenje žganega apna.It is an object of the present invention to provide a process for separating gas pollutants from hot process gases in which slaked lime can be replaced with calcined lime without the need for an expensive, special calcined lime quenching plant.
Po izumu je ta cilj dosežen s postopkom take vrste, kot je opredeljen v uvodu in ki je značilen po tem, da žgano apno dodajamo kot sveže vpojno gradivo in da glavni del prahu, ločenega v separatorju za prah, dodajamo v mešalnik in ga odvajamo iz letega v toku, ki je v bistvu neprekinjen, pri čemer prah tako dolgo zadržujemo v mešalniku in ga tolikokrat recirkuliramo, da je celotni čas zadrževanja žganega apna v mešalniku v navlaženem stanju zadosti dolg, da je žganemu apnu dan čas za reagiranje v bistvu popolnoma z vodo, dodajano v mešalnik, in za nastajanje gašenega apna.According to the invention, this object is achieved by a process as defined in the introduction, characterized in that the calcined lime is added as fresh absorbent material and that the main part of the powder separated in the dust separator is added to the mixer and removed from the mixer. cast in a stream that is substantially continuous, keeping the powder in the mixer for so long and recirculating so many times that the total retention time of the calcined lime in the agitator is long enough to allow the calcined lime to react substantially completely with water added to the mixer and to produce slaked lime.
Sveže vpojno gradivo v obliki žganega apna uvajamo prednostno v mešalnik, lahko pa ga tudi dodajamo tistemu delu prahu, ločenega v separatorju za prah, ki ga pošiljamo v mešalnik. Alternativno lahko žgano apno uvajamo neposredno v dimne pline v kontaktnem reaktorju.Preferably, the fresh absorbent material in the form of calcined lime is introduced into the mixer, but it can also be added to that part of the powder separated in the powder separator that is sent to the mixer. Alternatively, calcined lime can be introduced directly into the flue gas in the contact reactor.
V mešalnik smotrno uvajamo tok zraka, da se prah, ki se tam meša, fluidizira in se tako zmes zboljša.The flow of air is expediently introduced into the mixer in order to fluidize the powder therein and improve the mixture.
Izum bomo zdaj v podrobnostih opisali ob pomoči priložene skice, ki shematično kaže postrojenje za čiščenje dimnih plinov iz naprave za centralno ogrevanje na premog, pri čemer je čistilno postrojenje opremljeno z opremo za izvedbo postopka po pričujočem izumu.The invention will now be described in detail by way of the accompanying drawing, which schematically shows a flue gas purification plant from a coal fired central heating apparatus, the purification plant being provided with the equipment for carrying out the process of the present invention.
Skica shematično ponazarja postrojenje za čiščenje dimnih plinov iz naprave 1 za centralno ogrevanje na premog, pri čemer omenjeni dimni plini vsebujejo prah, kot je leteči pepel, in plinske onesnaževalce, kot je žveplov dioksid. Za prenos toplote iz vročih dimnih plinov v zgorevalni zrak, ki se napravi 1 za centralno ogrevanje dovaja s pomočjo puhala 3, je predvidena predgrevalna naprava 2.The sketch schematically illustrates a flue gas purification plant from a coal-fired central heating installation 1, said flue gases containing dust such as fly ash and gas pollutants such as sulfur dioxide. For the transfer of heat from hot flue gas to the combustion air supplied to the central heating system 1 by means of a blower 3, a preheating device 2 is provided.
Vroči dimni plini so speljani po kanalu 4 v separator 5 za prah, kije v predstavljenem izvedbenem primeru elektrostatični precipitator, ki ima tri zaporedne posedalne enote, skozi katere so vodeni dimni plini, ki se čistijo. Tako očiščeni dimni plini preko kanala 6 potujejo v puhalo 7 za dimne pline, ki jih preko kanala 8 pošilja v dimnik 9, da odtekajo v ozračje. Separator za prah je tudi lahko vrečni filter.The hot flue gases are channeled through channel 4 to a dust separator 5, which in the present embodiment is an electrostatic precipitator having three consecutive settling units through which the flue gases to be purged are guided. The purified flue gases via duct 6 travel to the flue gas blower 7, which through the duct 8 sends them to the chimney 9 to drain into the atmosphere. A dust separator can also be a bag filter.
Kanal 4 obsega pokončen odsek, ki tvori kontaktni reaktor 10. V spodnjem odseku kompaktnega reaktorja 10 s slednjim sodeluje mešalnik 11. Mešalnik 11 uvaja vpojno gradivo v obliki delcev, ki reagira s plinskimi onesnaževalci v dimnih plinih, v navlaženem stanju v dimne pline v spodnjem odseku kontaktnega reaktorja 10. To vpojno gradivo pretvarja plinske onesnaževalce v prah, ki se izloča v precipitatorju 5.Channel 4 comprises an upright section forming a contact reactor 10. In the lower section of the compact reactor 10, the mixer cooperates with the latter 11. The mixer 11 introduces absorbent particulate material that reacts with the flue gas pollutants in a moistened state into the flue gases in the lower section of contact reactor 10. This absorbent material converts gas pollutants into dust which is excreted in the precipitator 5.
Delci prahu, ločeni v precipitatorju 5, se zbirajo v vsipalnikih 12 precipitatorjevih enot. Glavni del zbranih delcev prahu se recirkulira v sistem na način, ki bo pobliže opisan spodaj. Preostanek zbranih delcev prahu se transportira stran na način, ki ga v podrobnostih ne opisujemo, denimo s pomočjo polžnega transporterja.Dust particles separated in the precipitator 5 are collected in the spreaders of the 12 precipitator units. The main part of the collected dust particles is recirculated into the system in a way that is described in more detail below. The remainder of the collected dust particles are transported away in a manner not described in detail, for example by means of a screw conveyor.
Mešalnik 11 je take vrste, kot je opisan v SE 9404104-3 (ekvivalent; SI _A). Torej, mešalnik 11 je v osnovi zasnovan kot škatla z dvema podoma. Med podoma, od katerih zgornji pod sestoji iz napetega fluidizacijskega blaga 13 iz poliestra, se nahaja komora 14, v katero preko voda 15 za dovod zraka dovajamo zrak za fluidiziranje vpojnega gradiva v obliki delcev v mešalniku 11. Vodo dovajamo v mešalnik 11 preko vodovodne napeljave 16 in šob 17, ki so razporejene v zgornjem odseku mešalnika. Gradivo v obliki delcev, ki gaje treba mešati, vnašamo v mešalnik 11 skozi dva materialna vpusta 18 in 19 na vstopnem koncu mešalnika. Mešalnik 11 nadalje obsega mehanski mešalni mehanizem 20, ki sestoji iz dveh sodelujočih vzporednih mešal (samo eno od njiju je nakazano na skici), s tem da ima vsako od njiju vodoravno gred in na njima pritrjenih več nagnjenih elipsastih kolutov. Izstopni konec mešalnika 11 sega v kontaktni reaktor 10, da vanj neprekinjeno vnaša preko preliva 21 dobro zmešano navlaženo vpojno gradivo.The mixer 11 is of the type described in SE 9404104-3 (equivalent; SI _ A ). So mixer 11 is basically designed as a box with two floors. Between the floors, the upper floor of which consists of a tensile fluidized bed 13 of polyester, there is a chamber 14 into which, through the air supply duct 15, air is supplied to fluidize the absorbent particulate material in the mixer 11. The water is fed to the mixer 11 via a plumbing fixture. 16 and nozzles 17 arranged in the upper section of the mixer. The particulate material to be mixed is introduced into the mixer 11 through two material inlets 18 and 19 at the inlet end of the mixer. The mixer 11 further comprises a mechanical mixing mechanism 20 consisting of two cooperating parallel mixers (only one of which is shown in the drawing), each having a horizontal shaft and several tilting ellipse rings attached to them. The outlet end of the mixer 11 extends into the contact reactor 10 to continuously inject well mixed absorbent absorbent material through the overflow 21.
Tisti del prašnih delcev, zbranih v vsipalnikih 12 precipitatorjevih enot, ki naj bo recirkuliran v sistem, se dovaja v mešalnik 11 preko vpusta 19. Žgano apno (kalcijev oksid) v obliki delcev dovajamo v mešalnik 11 preko vpusta 18 in ga zamešamo z delci prahu, dovedenimi preko vpusta 19. Zmes navlažimo z vodo, dovedeno preko šob 17. Vodo po šobah 17 dovajamo tudi za potrebe gašenja žganega apna, ki prihaja v mešalnik 11. Zahvaljujoč zgradbi mehanskega mešalnega mehanizma 20 in fluidizaciji materialnih delcev, prihajajočih v mešalnik 11, slednji ustvarjaThat part of the dust particles collected in the hoppers 12 of the precipitator units to be recirculated into the system is fed into the mixer 11 via inlet 19. The particulate calcined lime (calcium oxide) is fed into the mixer 11 via the inlet 18 and mixed with dust particles. supplied via inlet 19. The mixture is moistened with water supplied through the nozzles 17. Water is also fed through the nozzles 17 for the needs of extinguishing calcined lime entering the mixer 11. Thanks to the construction of the mechanical mixing mechanism 20 and the fluidization of the material particles entering the mixer 11, the latter creates
1. Akt Patentne pisarne d.o.o.: 25S32.1. Patent Office Act d.o.o .: 25S32.
enakomerno navlaženo homogeno zmes materialnih delcev, ki preko preliva 21 mešalnika 11 neprekinjeno dotekajo v kontaktni reaktor 10 kot vpojno gradivo. Čas zadrževanja materialnih delcev v mešalniku ll je velikostnega reda 5-60 s, smotrnoa uniformly moistened homogeneous mixture of particulate matter which flows continuously into the contact reactor 10 through the overflow 21 of the mixer 11 as absorbent material. The residence time of the particulate matter in the mixer 11 is in the order of 5-60 s, preferably
10-20 s.10-20 s.
Čas zadrževanja, kot je naveden zgoraj (10-20 s), materialnih delcev v mešalniku 11, t.j. čas, v katerem so delci apna v navlaženem stanju, ne zadošča, da bi žgano apno v celoti reagiralo z vodo, ki jo dodajamo za gašenje in izdelavo gašenega apna. Tovrstna reakcija je sorazmerno počasna in traja več minut.The residence time, as indicated above (10-20 s), of the material particles in the mixer 11, i.e. the time during which the lime particles are in a moistened state is not sufficient for the calcined lime to fully react with the water added to extinguish and produce the slaked lime. This reaction is relatively slow and takes several minutes.
Izum bomo zdaj opisali bolj v podrobnostih s pomočjo spodaj navedenega teoretičnega primera. V primeru so zajete razmere, kakršne obstajajo v točkah A, B in C s skice, t.j. v kanalu 4 pred mešalnikom 11, v reaktorju 10 za mešalnikom 11 na vhodu precipitatorja 5 oziroma na izhodu iz precipitatorja 5.The invention will now be described in more detail by way of the following theoretical example. In the case, the situation as in points A, B and C of the sketch is captured, i.e. in channel 4 in front of mixer 11, in reactor 10 behind mixer 11 at the inlet of the precipitator 5 or at the outlet of the precipitator 5.
Prah pri A je v bistvu leteči pepel, medtem ko je prah pri B leteči pepel skupaj z vpojnim gradivom.The dust at A is essentially fly ash, while the dust at B is fly ash along with absorbent material.
Pri D je iztekalo 2.930 kg prahu na uro, pri čemer je bilo 2.000 kg letečega pepela.At D, 2,930 kg of dust per hour leaked, leaving 2,000 kg of fly ash.
V tem primeru je torej vpojno gradivo v obliki delcev, ki je vsebovalo žgano apno, ki se je gasilo, krožilo povprečno okoli 35-krat (1,0 x 103.933 / 2.930 ~ 35) v sistemu, predenje pri D izteklo. Skupni čas zadrževanja vpojnega gradiva v mešalniku tako znaša 350-700 s, t.j. velikostnega reda 6-12 min, kar zadošča za to, da ima žgano apno čas za ugasitev.In this case, then, the absorbent particulate material containing the calcined lime which was extinguished circulated on average about 35 times (1.0 x 103.933 / 2.930 ~ 35) in the system, spinning at D expired. The total residence time of the absorbent material in the mixer is thus 350-700 s, i.e. size 6-12 min, which is sufficient for the calcined lime to have time to extinguish.
Skupna poraba vode v zgornjem primeru je 3.366 1/h. od česar je 152 1/h potrebne za gašenje apna. Ko je ta količina vode porabljena, znaša vsebnost vlage vpojnega gradiva na iztoku iz mešalnika 11 okoli 6%. Vsebnost vlage pa se v odvisnosti od sestave zmesi lahko spreminja v območju 2-15%.The total water consumption in the example above is 3.366 1 / h. of which 152 l / h is required for lime quenching. When this amount of water is consumed, the moisture content of the absorbent material at the outlet of the mixer 11 is about 6%. However, depending on the composition of the mixture, the moisture content can vary in the range of 2-15%.
Če je v zgornjem primeru vsebnost letečega pepela v dimnih plinih pri točki A ničelna, t.j. iztok pri točki D znaša 930 kg/h, bo število obkrožitev po analogiji z zgoraj navedeno znašala okoli 110 (0,980 x 103.993 / 930 « 110), tako da tedaj čas zadrževanja znaša 1.100-2.200 s, t.j. velikostnega reda 18-37 min.If, in the above example, the fly ash content of the flue gas at point A is zero, i.e. the outflow at point D is 930 kg / h, the number of encirclement by analogy with the above will be about 110 (0.980 x 103.993 / 930 «110), so that the residence time is then 1,100-2,200 s, i.e. size order 18-37 min.
Claims (5)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE9404105A SE504440C2 (en) | 1994-11-28 | 1994-11-28 | Ways to separate gaseous pollutants from hot process gases |
| PCT/SE1995/001403 WO1996016722A1 (en) | 1994-11-28 | 1995-11-24 | Method for separating gaseous pollutants from hot process gases |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| SI9520141A true SI9520141A (en) | 1997-10-31 |
Family
ID=20396125
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| SI9520141A SI9520141A (en) | 1994-11-28 | 1995-11-24 | Method for separating gaseous pollutants from hot process gases |
Country Status (20)
| Country | Link |
|---|---|
| EP (1) | EP0804273A1 (en) |
| JP (1) | JP3640674B2 (en) |
| KR (1) | KR100384589B1 (en) |
| CN (1) | CN1080137C (en) |
| AU (1) | AU692014B2 (en) |
| BR (1) | BR9509831A (en) |
| CZ (1) | CZ157497A3 (en) |
| EE (1) | EE04049B1 (en) |
| FI (1) | FI972233A (en) |
| HU (1) | HU220402B (en) |
| MD (1) | MD1020C2 (en) |
| PL (1) | PL320426A1 (en) |
| RO (1) | RO115421B1 (en) |
| RU (1) | RU2147919C1 (en) |
| SE (1) | SE504440C2 (en) |
| SI (1) | SI9520141A (en) |
| SK (1) | SK66197A3 (en) |
| UA (1) | UA52592C2 (en) |
| WO (1) | WO1996016722A1 (en) |
| ZA (1) | ZA959876B (en) |
Families Citing this family (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT404565B (en) * | 1997-06-05 | 1998-12-28 | Scheuch Alois Gmbh | METHOD FOR PURIFYING POLLUTANT-GASES |
| SE514592C2 (en) * | 1998-05-18 | 2001-03-19 | Flaekt Ab | Method and apparatus for flue gas purification with extinguishing lime in immediate connection with flue gas purification |
| SE512227C2 (en) * | 1998-06-24 | 2000-02-14 | Flaekt Ab | Ways to clean flue gases during the start-up of a boiler |
| US6290921B1 (en) * | 1999-11-03 | 2001-09-18 | Foster Wheeler Enegeria Oy | Method and apparatus for binding pollutants in flue gas |
| SE523667C2 (en) | 2002-09-20 | 2004-05-11 | Alstom Switzerland Ltd | Method and apparatus for separating gaseous pollutants from hot gases by particulate absorbent material and mixer for wetting the absorbent material |
| ATE403487T1 (en) | 2006-02-06 | 2008-08-15 | Alstom Technology Ltd | METHOD AND DEVICE FOR CONTROLLING THE ABSORPTION OF GASEOUS IMPURITIES FROM HOT PROCESS GASES |
| DE602006020030D1 (en) | 2006-07-04 | 2011-03-24 | Alstom Technology Ltd | Method and device for separating gaseous pollutants from hot exhaust gases |
| AT504426B8 (en) * | 2006-10-24 | 2008-09-15 | Scheuch Gmbh | APPARATUS FOR MOISTURIZING A SORPTION AGENT |
| US7766997B2 (en) | 2007-12-21 | 2010-08-03 | Alstom Technology Ltd | Method of reducing an amount of mercury in a flue gas |
| US7850936B2 (en) | 2008-02-18 | 2010-12-14 | Alstom Technology Ltd | Dry sulfur dioxide (SO2) scrubbing |
| CN101513589B (en) * | 2009-03-03 | 2011-07-20 | 桑德环境资源股份有限公司 | Method and device for purification of flue gases by semidry process |
| US8192529B2 (en) * | 2009-03-10 | 2012-06-05 | Gatton Jr Lawrence H | Integrated dry scrubber system |
| ES2593812T3 (en) | 2010-11-24 | 2016-12-13 | General Electric Technology Gmbh | Method of purifying a combustion gas rich in carbon dioxide and a boiler system |
| US8728211B2 (en) | 2012-03-30 | 2014-05-20 | Alstom Technology Ltd | Nozzle for spraying liquid and a mixer comprising the nozzle |
| US9457366B2 (en) * | 2012-07-13 | 2016-10-04 | General Electric Technology Gmbh | Spray lance arrangement |
| US8663586B1 (en) | 2012-08-07 | 2014-03-04 | Alstom Technology Ltd | High performance mercury capture |
| US9108152B2 (en) * | 2013-11-26 | 2015-08-18 | Alstom Technology Ltd | Dry scrubber system with low load distributor device |
| US8906333B1 (en) * | 2013-11-27 | 2014-12-09 | Alstom Technology Ltd | Dry scrubber system with air preheater protection |
| CN105617851B (en) * | 2016-03-16 | 2018-08-28 | 中国科学院城市环境研究所 | A kind of method and its device of efficient double tower semi-dry desulphurization |
| JP7360378B2 (en) * | 2017-09-06 | 2023-10-12 | エス．ア．ロイスト ルシェルシュ エ デヴロップマン | Method of treating exhaust gas in CDS exhaust gas treatment |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3308927A1 (en) | 1983-03-12 | 1984-09-13 | L. & C. Steinmüller GmbH, 5270 Gummersbach | Process for binding gaseous pollutants contained in flue gases |
| SE453570B (en) * | 1985-10-09 | 1988-02-15 | Flaekt Ab | Plant for sepg. acid components from gas mixt. |
| SE458095B (en) * | 1986-06-27 | 1989-02-27 | Flaekt Ab | Sepn. system for pollutants from gas-form medium |
| FI76931B (en) * | 1986-12-12 | 1988-09-30 | Imatran Voima Oy | FOERFARANDE FOER RENING AV ROEKGASER. |
| JP3035015B2 (en) * | 1991-08-13 | 2000-04-17 | 三菱重工業株式会社 | Desulfurization method |
-
1994
- 1994-11-28 SE SE9404105A patent/SE504440C2/en not_active IP Right Cessation
-
1995
- 1995-11-21 ZA ZA959876A patent/ZA959876B/en unknown
- 1995-11-24 MD MD97-0166A patent/MD1020C2/en unknown
- 1995-11-24 CZ CZ971574A patent/CZ157497A3/en unknown
- 1995-11-24 WO PCT/SE1995/001403 patent/WO1996016722A1/en active IP Right Grant
- 1995-11-24 PL PL95320426A patent/PL320426A1/en unknown
- 1995-11-24 RO RO97-00951A patent/RO115421B1/en unknown
- 1995-11-24 EE EE9700215A patent/EE04049B1/en not_active IP Right Cessation
- 1995-11-24 KR KR1019970703389A patent/KR100384589B1/en not_active IP Right Cessation
- 1995-11-24 RU RU97111848A patent/RU2147919C1/en not_active IP Right Cessation
- 1995-11-24 BR BR9509831A patent/BR9509831A/en not_active IP Right Cessation
- 1995-11-24 CN CN95196504A patent/CN1080137C/en not_active Expired - Lifetime
- 1995-11-24 AU AU41264/96A patent/AU692014B2/en not_active Ceased
- 1995-11-24 HU HU9800501A patent/HU220402B/en not_active IP Right Cessation
- 1995-11-24 JP JP51717096A patent/JP3640674B2/en not_active Expired - Lifetime
- 1995-11-24 SK SK661-97A patent/SK66197A3/en unknown
- 1995-11-24 SI SI9520141A patent/SI9520141A/en not_active IP Right Cessation
- 1995-11-24 EP EP95939455A patent/EP0804273A1/en not_active Withdrawn
- 1995-11-24 UA UA97063196A patent/UA52592C2/en unknown
-
1997
- 1997-05-27 FI FI972233A patent/FI972233A/en not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| BR9509831A (en) | 1997-09-30 |
| JPH10509914A (en) | 1998-09-29 |
| ZA959876B (en) | 1996-07-15 |
| RU2147919C1 (en) | 2000-04-27 |
| KR100384589B1 (en) | 2003-08-21 |
| SE504440C2 (en) | 1997-02-10 |
| WO1996016722A1 (en) | 1996-06-06 |
| EE04049B1 (en) | 2003-06-16 |
| SK66197A3 (en) | 1997-10-08 |
| HUT77637A (en) | 1998-06-29 |
| RO115421B1 (en) | 2000-02-28 |
| CZ157497A3 (en) | 1997-11-12 |
| CN1167450A (en) | 1997-12-10 |
| SE9404105L (en) | 1996-05-29 |
| UA52592C2 (en) | 2003-01-15 |
| HU220402B (en) | 2002-01-28 |
| PL320426A1 (en) | 1997-09-29 |
| MD1020C2 (en) | 1999-07-31 |
| FI972233A0 (en) | 1997-05-27 |
| JP3640674B2 (en) | 2005-04-20 |
| EP0804273A1 (en) | 1997-11-05 |
| AU4126496A (en) | 1996-06-19 |
| FI972233A (en) | 1997-05-27 |
| AU692014B2 (en) | 1998-05-28 |
| CN1080137C (en) | 2002-03-06 |
| EE9700215A (en) | 1998-02-16 |
| SE9404105D0 (en) | 1994-11-28 |
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Legal Events
| Date | Code | Title | Description |
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| IF | Valid on the event date | ||
| KO00 | Lapse of patent |
Effective date: 20060731 |