AU4126496A - Method for separating gaseous pollutants from hot process gases - Google Patents
Method for separating gaseous pollutants from hot process gasesInfo
- Publication number
- AU4126496A AU4126496A AU41264/96A AU4126496A AU4126496A AU 4126496 A AU4126496 A AU 4126496A AU 41264/96 A AU41264/96 A AU 41264/96A AU 4126496 A AU4126496 A AU 4126496A AU 4126496 A AU4126496 A AU 4126496A
- Authority
- AU
- Australia
- Prior art keywords
- mixer
- dust
- process gases
- supplied
- burnt lime
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims description 34
- 239000007789 gas Substances 0.000 title claims description 21
- 239000003344 environmental pollutant Substances 0.000 title claims description 13
- 231100000719 pollutant Toxicity 0.000 title claims description 12
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 45
- 239000000428 dust Substances 0.000 claims description 37
- 239000000292 calcium oxide Substances 0.000 claims description 24
- 235000012255 calcium oxide Nutrition 0.000 claims description 24
- 239000002250 absorbent Substances 0.000 claims description 21
- 230000002745 absorbent Effects 0.000 claims description 21
- 239000003546 flue gas Substances 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 9
- 239000000920 calcium hydroxide Substances 0.000 claims description 9
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 9
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 9
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 7
- 235000010269 sulphur dioxide Nutrition 0.000 claims description 3
- 239000004291 sulphur dioxide Substances 0.000 claims description 3
- 239000002245 particle Substances 0.000 description 11
- 239000012716 precipitator Substances 0.000 description 7
- 239000010881 fly ash Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 3
- 235000011941 Tilia x europaea Nutrition 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000004571 lime Substances 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 101100345589 Mus musculus Mical1 gene Proteins 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000008240 homogeneous mixture Substances 0.000 description 1
- 239000011236 particulate material Substances 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 239000002594 sorbent Substances 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
- B01D53/46—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
Description
METHOD FOR SEPARATING GASEOUS POLLUTANTS FROM HOT PROCESS GASES
The present invention relates to a method for sepa¬ rating gaseous pollutants, such as sulphur dioxide, from hot process gases, such as flue gases, in which method the process gases are passed through a contact reactor, in which a particulate absorbent material, which is reac¬ tive with the gaseous pollutants, is introduced in mois¬ tened state into the process gases for converting the gaseous pollutants into separable dust, whereupon the process gases are passed through a dust separator, in which dust is separated from the process gases and from which the cleaned process gases are discharged, part of the dust separated in the dust separator being passed to a mixer, in which it is mixed and supplied with water so as to be moistened, whereupon it is recirculated as ab- sorbent material by being introduced into the process gases together with an addition of fresh absorbent.
The above-described method for separating gaseous pollutants from hot process gases is known from e.g. SE 8504675-3 and SE 8904106-5. According to these two docu- ments, use is preferably made of slaked lime (calcium hydroxide) in particle form as fresh absorbent. This absorbent is mixed with dust which has been separated from the process gases in the dust separator, whereupon the mixture is supplied with water to be introduced, in moistened state, into the flue gases in the contact reac¬ tor. The slaked lime is comparatively expensive, and so various experiments have been made to use burnt lime (calcium oxide) instead, which is considerably less ex¬ pensive. In these experiments, a plant had to be used, in which the burnt lime has first been slaked, i.e. the calcium oxide has been caused to react with water to form calcium hydroxide, before being introduced into the cleaning process. Such a lime slaking plant is expensive,
which means that the expected profit when changing from slaked lime to burnt lime failed to appear.
The object of the present invention is to provide a method for separating gaseous pollutants from hot process gases, in which the slaked lime can be replaced by burnt lime, without necessitating an expensive, separate plant for slaking the burnt lime.
According to the invention, this object is achieved by a method which is of the type mentioned by way of in- troduction and is characterised in that burnt lime is added as fresh absorbent, and that the major part of the dust separated in the dust separator is supplied to and discharged from the mixer in a substantially continuous flow, the dust being kept so long in the mixer and being recirculated so many times that the total residence time of the burnt lime in the mixer in moistened state is suf¬ ficiently long for the burnt lime to have time to react substantially completely with water supplied to the mixer and form slaked lime. The fresh absorbent in the form of burnt lime is supplied preferably to the mixer, but it may also be added to that part of the dust separated in the dust separator which is supplied to the mixer. Alternatively, the burnt lime can be introduced directly into the flue gases in the contact reactor.
An air flow is suitably supplied to the mixer in order to fluidise the dust mixed therein and thus improve the mixture.
The invention will now be described in more detail with reference to the accompanying drawing, which schema¬ tically illustrates a plant for cleaning flue gases from a coal-fired central heating plant, the cleaning plant being provided with equipment for carrying out the method according to the present invention. The drawing schematically illustrates a plant for cleaning flue gases from a coal-fired central heating plant 1, said flue gases containing dust, such as fly
ash, and gaseous pollutants, such as sulphur dioxide. A preheating device 2 is arranged to transmit heat from the hot flue gases to combustion air, which via a duct 2a is supplied to the central heating plant 1 by means of a fan 3.
The hot flue gases are conveyed through a duct 4 to a dust separator 5, which in the embodiment shown is an electrostatic precipitator having three successive preci- pitator units, through which the flue gases are passed to be cleaned. The flue gases cleaned in this manner are via a duct 6 passed to a flue gas fan 7, which via a duct 8 feeds them on to a chimney 9 to be emitted into the at¬ mosphere. The dust separator can also be a bag filter.
The duct 4 comprises a vertical portion which forms a contact reactor 10. A mixer 11 communicates with the contact reactor 10 in the lower part thereof. The mixer 11 introduces a particulate absorbent material, which is reactive with the gaseous pollutants in the flue gases, in moistened state into the flue gases in the lower part of the contact reactor 10. This absorbent material con¬ verts the gaseous pollutants into dust, which is separat¬ ed in the precipitator 5.
The dust particles separated in the precipitator 5 are collected in the hoppers 12 of the precipitator units. The major part of the collected dust particles is recirculated in the system in a manner which will be described in detail below. The remainder of the collect¬ ed dust particles are transported away in a manner which will not be described in detail, for instance by means of a worm conveyor.
The mixer 11 is of the type as described in SE- 9404104-3. Thus, the mixer 11 has essentially the shape of a double-bottom box. Between the two bottoms, the upper of which consists of a tensioned fluidising cloth 13 of polyester, there is a chamber 14, to which air for fluidising the particulate absorbent material in the mixer 11 is conducted through an air supply conduct 15.
Water is supplied to the mixer 11 through a water supply conduit 16 and nozzles 17, which are arranged in the upper portion of the mixer. The particulate material which is to be mixed, is supplied to 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 agi¬ tators (of which only one is shown in the drawing), each having a horizontal shaft and, mounted thereon, a plura- lity of inclined elliptic plates. The outlet end of the mixer 11 extends into the contact reactor 10 in order to continuously supply thereto through an overflow 21 well- mixed, moistened absorbent material.
That part of the dust particles collected in the hoppers 12 of the precipitator units which is to be recirculated in the system is supplied to the mixer 11 through the inlet 19. Particulate burnt lime (calcium oxide) is supplied to the mixer 11 through the inlet 18 to be mixed with the dust particles supplied through the inlet 19. The mixture is moistened with water supplied through the nozzles 17. Water is supplied through the nozzles 17 also in order to slake the burnt lime supplied to the mixer 11. Owing to the construction of the mecha¬ nical mixing mechanism 20 and the fluidisation of the material particles supplied to the mixer 11, the mixer produces a homogeneously moistened, homogeneous mixture of material particles, which are, through the overflow 21 of the mixer 11, continuously supplied to the contact reactor 10 as absorbent material. The residence time of the material particles in the mixer 11 is in the order of 5-60 s, especially 10-20 s.
The residence time as stated above (10-20 s) of the material particles in the mixer 11, i.e. the time during which the lime particles are in moistened state, is in- sufficient for the burnt lime to have time to react com¬ pletely with the water added for slaking and form slaked
lime. Such a reaction is relatively slow and takes seve¬ ral minutes.
The invention will now be described in more detail with the aid of the theoretical Example below. The Exam- pie states the conditions prevailing at points A, B and C in the drawing, i.e. in the duct 4 before the mixer 11, in the reactor 10 after the mixer 11 at the inlet of the precipitator 5 and at the outlet of the precipitator 5, respectively.
A B C
Gas flow (Nm3/h) 100,000 103,993 103, ,993 Gas temperature ( cC) 125 65 65 S02 concentration (ppm) 1,150 280 172 Dust concentration (g/Nm3) 20 1,000 < 0. ,03
The dust at A is substantially fly ash, whereas the dust at B is fly ash and absorbent material.
At D, 2,930 kg of dust are discharged per hour, 2,000 kg being fly ash.
In this Example, the particulate absorbent mate¬ rial, including the burnt lime, which is being slaked, is thus circulated on the average about 35 times (1.0 x 103,933 / 2,930 * 35) in the system before being discharged at D. The total residence time of the absor¬ bent material in the mixer 11 thus is 350-700 s, i.e. in the order of 6-12 min, which is sufficient for the burnt lime to have time to be slaked.
The total consumption of water in the above Example is 3,366 1/h, of which 152 1/h is required for the slak¬ ing of lime. When this amount of water is consumed, the moisture content of the absorbent material discharged from the mixer 11 is about 6%. However, the moisture con¬ tent can, according to the composition of the mixture, suitably be varied in the range 2-15%.
If, in the above Example, the fly ash content of the flue gases at point A is zero, i.e. the discharge at D is
930 kg/h, the circulation number will, by analogy with that stated above, be about 110 (0.980 x 103,993 / 930 * 110), which in turn yields a residence time of 1,100-2,200 s, i.e. in the order of 18-37 min.
Claims (5)
1. A method for separating gaseous pollutants, such as sulphur dioxide, from hot process gases, such as flue gases, in which method the process gases are passed through a contact reactor (10), in which a particulate absorbent material, which is reactive with the gaseous pollutants, is introduced in moistened state into the process gases for converting the gaseous pollutants into separable dust, whereupon the process gases are passed through a dust separator (5), in which dust is separated from the process gases and from which the cleaned process gases are discharged, part of the dust separated in the dust separator (5) being passed to a mixer (11), in which it is mixed and supplied with water so as to be moisten¬ ed, whereupon it is recirculated as absorbent material by being introduced into the process gases together with an addition of fresh absorbent, c h a r a c t e r i s e d in that burnt lime is added as fresh absorbent, and that the major part of the dust separated in the dust separator (5) is supplied to and discharged from the mixer (11) in a substantially continuous flow, the dust being kept so long in the mixer and being recirculated so many times that the total residence time of the burnt lime in the mixer (11) in moistened state is sufficiently long for the burnt lime to have time to react substantially com¬ pletely with water supplied to the mixer and form slaked lime.
2. The method as claimed in claim 1, c h a r a c ¬ t e r i s e d in that the fresh absorbent in the form of burnt lime is supplied to the mixer (11).
3. The method as claimed in claim 1, c h a r a c ¬ t e r i s e d in that the fresh absorbent in the form of burnt lime is added to that part of the dust separated in the dust separator ( 5) which is supplied to the mixer (11).
4. The method as claimed in claim 1, c h a r a c ¬ t e r i s e d in that the fresh absorbent in the form of burnt lime is introduced directly into the flue gases in the contact reactor (10).
5. The method as claimed in any one of the preceding claims, c h a r a c t e r i s e d in that an air flow is supplied to the mixer (11) in order to fluidise the dust mixed therein.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE9404105 | 1994-11-28 | ||
| 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 (2)
| Publication Number | Publication Date |
|---|---|
| AU4126496A true AU4126496A (en) | 1996-06-19 |
| AU692014B2 AU692014B2 (en) | 1998-05-28 |
Family
ID=20396125
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU41264/96A Ceased AU692014B2 (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 |
Family Cites Families (5)
| 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 |
| SI9520141A (en) | 1997-10-31 |
| 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 |
| 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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