CN1125911A - The treatment of gaseous substances - Google Patents
The treatment of gaseous substances Download PDFInfo
- Publication number
- CN1125911A CN1125911A CN95190224A CN95190224A CN1125911A CN 1125911 A CN1125911 A CN 1125911A CN 95190224 A CN95190224 A CN 95190224A CN 95190224 A CN95190224 A CN 95190224A CN 1125911 A CN1125911 A CN 1125911A
- Authority
- CN
- China
- Prior art keywords
- solution
- tower
- loop
- extractant
- aqueous solution
- 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
- 239000000126 substance Substances 0.000 title claims abstract description 7
- 239000000243 solution Substances 0.000 claims abstract description 61
- 239000002253 acid Substances 0.000 claims abstract description 41
- 238000000034 method Methods 0.000 claims abstract description 25
- 230000002378 acidificating effect Effects 0.000 claims abstract description 23
- 239000007864 aqueous solution Substances 0.000 claims abstract description 23
- 239000000463 material Substances 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 19
- 239000000284 extract Substances 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims description 2
- 239000013505 freshwater Substances 0.000 claims description 2
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims description 2
- 239000006259 organic additive Substances 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 239000011261 inert gas Substances 0.000 claims 1
- 238000003672 processing method Methods 0.000 claims 1
- 238000000605 extraction Methods 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000004615 ingredient Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 230000032258 transport Effects 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 230000026030 halogenation Effects 0.000 description 1
- 238000005658 halogenation reaction Methods 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910001510 metal chloride Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
Images
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
- B01D53/14—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 by absorption
- B01D53/1456—Removing acid components
-
- 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
- B01D53/14—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 by absorption
-
- 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
- B01D53/14—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 by absorption
- B01D53/1406—Multiple stage absorption
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a method for the treatment of a gaseous acidic substance which includes delivering the said substance to a packed tower or scrubber in which the gaseous acidic substance is intimately contacted with a supply of a dilute aqueous extractant solution, the tower being in an extractant solution recirculation loop in which extractant solution is delivered to the tower and is removed from the tower and the concentration of acid in solution in the loop is maintained in an acid concentration range by addition of dilute aqueous solution to the loop and the extraction of aqueous solution of greater acidic concentration from the loop.
Description
The present invention relates to the processing of gaseous material, particularly by the acid smog that generates as the chemical reaction in chemical process factory.
The feature that many organic and non-organic chemistry are handled is to generate acid product, they or primary product or accessory substance.The common example of Chu Liing comprises the halogenation of aromatic like this, as the chlorination of benzene and the regeneration of acid, as in order to reclaim hydrochloric acid or sulfur dioxide respectively, metal chloride or sulfate is destroyed.
At present, the recovery of such acidic gaseous compound or in connecting the condenser of vent gas treatment is to reduce acid ingredient to environmentally acceptable level, perhaps not condensation on some degree.
Various methods all are used to realize above-mentioned target, are included in absorption in spray tower, stirred reactor, packed column (scrubber) and the spray tower.
A feature of a lot of these methods is that acid ingredient neutralizes with alkali, and normally with NaOH or potassium hydroxide or amine neutralization, then it is reproduced.
In packed column, acid absorbs and neutralization reaction takes place simultaneously, because reaction can produce high heat, difficulty also just occurs.This heat can destroy as packing material or be used to build the profile of the plastic material of packed column.And if feed composition is various, the control of reaction is complicated especially.
The purpose of this invention is to provide a kind of improving one's methods of gaseous state acidic materials of handling, it aforesaid shortcoming do not occur.
Can provide a kind of method that is used to handle the gaseous state acidic materials according to the present invention, it comprises transports described material in packed column or scrubber, therein, the gaseous state acidic materials closely contact with the feed of rare extractant aqueous solution, tower is in the extractant solution recirculation circuit, extractant solution is transported in the tower in recirculation circuit, and is removed from tower again.By adding dilute aqueous solution in the entry loop and from the loop, extracting the more aqueous solution of high acid concentration, the concentration of the acid of solution in the loop is maintained in certain acid concentration scope.
In the preferred form of the method according to this invention, described tower has an outlet that is used for discharging any remaining gaseous material that is not extracted at this tower.Any remaining gaseous material is transported to second packed column or scrubber, and in tower, the acidic gaseous material closely contacts with the feed of rare extractant aqueous solution.Second packed column is in second extractant solution recirculation circuit, and extractant solution is transported to second tower in recirculation circuit, and removes from second tower.By controlling the dilute aqueous solution that adds to second loop and from second loop, extracting the aqueous solution that contains any acidic materials that adds in the tower, the acid concentration of solution in second loop is maintained in second acid concentration scope.
In this method, first tower can be used for cushioning the variation of charge air flow concentration, and the gas stream of the substantial constant content of acid gas being provided for second tower.
Be added to the dilute aqueous solution in each recirculation circuit, can be water or contain one or more inorganic and/or organic additive solution, as enanthol less than 0.5 weight %.
Packed column or scrubber can be built by known method.Packing material can be any known inert solid material that high surface is arranged, and can use commercially availabie synthetic product or natural materials, as gravel, cobble.
Each recirculation circuit can comprise a reservoir that is used for recirculation solution.This reservoir can be the basin that is installed under the tower.By suitable water discharge method, solution can be discharged to basin from tower.On the reservoir in loop, fresh dilute aqueous solution can be added in each loop, as on the jar limit or near jar the top.Any aqueous solution that contains described acidic materials can be removed from each loop of reservoir back.
It is desirable to, by regulating the speed that fresh water solution adds the speed of recirculation circuit and extract acidic aqueous solution from the loop, make the acid concentration of solution in described each reservoir be controlled in the given concentration range (or substantial constant).Available suitable known fluid control device, as valve, optional relevant current meter is controlled above-mentioned adding and extraction separately.For example: in the reservoir in first extractant solution regeneration cycle loop, the acid concentration of extractant solution can maintain in 2~20 weight % scopes, as 5~12 weight %.Acid concentration in the extractant solution of second extractant solution loop can maintain in 0~2 weight % scope, as 0~0.5 weight %.
In each described recirculation circuit, all to use pump to transport extractant solution, the tower from the reservoir described in this loop to same circuit is as on the tower limit or near the top of tower.
The feed of inlet gaseous material can be added in each tower on the tower limit or near at the bottom of the tower.So feed can rise by the filler of tower, and the filler whereabouts that contacts by tower is the extractant liquid of seepage flow.
In each recirculation circuit, the recirculation of extractant solution can be carried out continuously.Begun to start and after desired acid concentration reaches (this can detect with the suitable pH detector means that is installed in the described reservoir) in each loop in process, extractant solution also can continue to join in the loop, and continue from the loop, to be removed, and keep concentration in claimed range, it is desirable to maintain the level of substantial constant.
This method according to the present invention can be a kind of suitable method, and in the method, the acidic gaseous material that is extracted is and one or more relevant accessory substances of non-acid gas that are processed separately or reclaim.For example, be transported to the feed of the acidic gaseous material in first tower of mentioning, can comprise described one or more non-acid gases.
Described non-acid gases can comprise that as hydrogen, the gaseous state acidic by-products comprises hydrogen fluoride.These gases can be chosen wantonly by inert carrier gas stream, deliver as nitrogen.
Compared with prior art, the present invention shows following useful and beyond thought advantage:
(a) there are not to cause being used to build the material of packed column or the reaction heat generation that filler wears out basically.
(b) volume that the heat of dilution can be by regulating reservoir and in each recirculation circuit removing of extractant solution with fill rate controlled.
(c) because extractant solution acid concentration is known, there is the packed column of suitable dimensions and contact performance accurately to be designed.
(d) because extractant solution acid concentration is maintained in the given range, if the acid concentration of the gas of supply stream changes, just can be not influential to the extraction performance that takes place subsequently.
(e) because the acid concentration of the extractant flow of solution of removing from recirculation circuit is known (or be controlled in the given scope and can measure), with regard to helping the air-flow of removing is for further processing, as fusion, storage or neutralization.
Embodiment of the present invention will be described by the method that has example with reference to the accompanying drawings:
Fig. 1 is the equipment block scheme that is used for removing from gas stream the acidic gaseous material by embodiment of the present invention.The equipment that shows among Fig. 1 can for example be used for from removing HF with nitrogen as the air-flow that contains HF and hydrogen of carrier gas.
As shown in Figure 1, be input to gas in the equipment is transported to first packed column 3 through piping 1 bottom 3a.Extractant solution through piping 4, is transported to the top 3b of tower 3 from end jar 7 by pump 5, and the gas in the pipeline 1 rises by packed column 3, and the extractant liquid that gets off by tower 3 seepage flow of contact.So the acid ingredient in air-flow is dissolved in the extractant solution.Extractant solution is collected at 3a place, the bottom of tower 3 and is flowed in the end jar 7 through piping 6, and the effect of end jar 7 is equivalent to the reservoir of this solution.Jar 7 is in the recirculation circuit that comprises tower 3, pipeline 6, jar 7 and pipeline 4.The fresh extractor agent solution, as water purification, the pipeline 9 through connecting control valve 11 joins the jar 7 from the jar upper end.Collect and pass through the extractant solution of pump 5 pump pressures at end jar 7 places, can discharge from the pipeline 13 of pipeline 4 through connecting control valve 15.The liquid level of the extractant solution of collecting in end jar 7 can be monitored through a suitable level monitoring instrument 17, and the pH of the solution in the jar 7 can monitor with monitor 19.
When using equipment shown in Figure 1, the acid concentration of the solution in end jar 7 allows to be increased to the scope of 5~12 weight %.When reaching this concentration, the speed that jar speed that 7 permissions are filled and solution flow out from pipeline 13 is regulated by valve 11,15, so the liquid level and the concentration of extractant solution are fixed in the jar 7.
Discharge gas in the tower 3 contains the residue sour gas of low concentration usually, can remove by another packed column 21, and tower 21 modes of action are similar to packed column 3.Discharge gas by pipeline 21, be transported to the bottom 21a of another tower 21 from the top 3b of tower 3.
Extractant solution is transported to the top 21b of tower 21 from end jar 27 through piping 24 by pump 25.Rise by packed column 21 from the gas of pipeline 20, and contact with extractant liquid that seepage flow from tower 21 gets off.So the acid ingredient in the gas stream is dissolved in the extractant solution.Extractant solution is collected at 21a place, the bottom of tower 21, and is discharged in the end jar 27 through piping 21, and the effect of end jar 27 is as the reservoir of this solution.Jar 27 is in the recirculation circuit that comprises tower 21, pipeline 26, jar 27 and pipeline 24.Fresh extractant solution as water purification, joins the jar 27 from the jar upper end by the pipeline 29 that is connecting control valve 31.Be collected in the extractant solution in the end jar 27,, can emit through the pipeline 33 that is connecting control valve 15 from pipeline 24 by pump 25 pump pressures.The liquid level of the extractant solution of collecting in end jar 27 is monitored by a suitable level sensor 37, and the pH of solution monitors with pH monitor 39 in the jar 27.
When using equipment shown in Figure 1, the acid concentration of solution allows to be increased in the end jar 27 to greatest extent in 0~0.5 weight % scope.After this valve 31,35 is used for regulating the liquid level that fixes end jar 27 extractant solution, and keeps acid concentration on the level that requires.
Clean non-acid gases extracts through connecting the outlet conduit 41 of pump 43 from the upper end of tower 21.
The liquid of emitting through piping 13 and 33 that is extracted can be transported in the storage tank, after this neutralizes in a usual manner with alkali.
Claims (12)
1. the processing method of acidic gaseous material, comprise and transport described material to packed column or scrubber, the gaseous state acidic materials closely contact with the feed of rare extractant aqueous solution there, this tower is in the recirculation circuit of extractant solution, extractant is transported in this tower and from this tower and removes in this loop, by in the loop, adding the dilute aqueous solution and the aqueous solution that from the loop, extracts bigger acid concentration, make that the acid concentration of solution maintains in certain acid concentration scope in the loop.
2. the method for claim 1, wherein said tower has an outlet that is used for any remaining gaseous material of not being extracted as yet at this tower, any remaining gaseous material is transported to second packed column or scrubber, the gaseous state acidic materials closely contact with the feed of rare extractant aqueous solution there, second packed column is in second extractant solution recirculation circuit, extractant solution is transported in second tower in this loop, and from second tower, remove, add dilute aqueous solution and from second loop, extract the aqueous solution that contains the acidic materials in any adding tower to second loop by control, the acid concentration of the aqueous solution in second loop is maintained in second acid concentration scope.
3. claim 1 or 2 method wherein add the dilute aqueous solution in or each recirculation circuit, are water or contain one or more solution inorganic and/or organic additive less than 0.5 weight %.
4. claim 1,2 or 3 method, one of them or each recirculation circuit comprises a reservoir that is used for recirculation solution, and this reservoir is installed on jar providing under the tower by one, and this solution is discharged in the jar from tower by drainage arrangement.
5. the method for claim 4, wherein fresh dilute aqueous solution on the jar limit or near jar the top, in the reservoir place in this loop was added into one or each loop, the aqueous solution that contains described acidic materials was removed from each loop behind reservoir.
6. claim 4, arbitrary method of 5 or 6, the speed that wherein joins the speed of the fresh water solution in the recirculation circuit and from the loop, extract acidic aqueous solution by adjusting, make the acid concentration control of solution in each described reservoir, to maintain in the given concentration range or the concentration value of substantial constant.
7. the method for claim 6, comprising first and second packed column, wherein, comprise in the reservoir of the first extractant solution recirculation circuit of first tower, the acid concentration of extractant solution maintains in 2~20% scopes, comprise that the acid concentration of extractant solution maintains in the 0-2% scope in the reservoir of the second extractant solution recirculation circuit of second tower.
8. the method in the claim of any one front, wherein the recirculation of the extractant solution in one or each recirculation circuit is carried out continuously.
9. the method in the claim of any one front, the acidic gaseous material that wherein is extracted is and the relevant accessory substance of one or more non-acid gases that is processed separately or reclaims.
10. the method in the claim 9, wherein said non-acid gases comprises hydrogen, acidic materials comprise hydrogen fluoride.
11. the method in claim 9 or 10, wherein gas delivers with inert gas flow.
12. in the claim 1 and substantially as preceding method with reference to the accompanying drawings.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB9402886.7 | 1994-02-15 | ||
GB9402886A GB9402886D0 (en) | 1994-02-15 | 1994-02-15 | The treatment of gaseous substances |
Publications (2)
Publication Number | Publication Date |
---|---|
CN1125911A true CN1125911A (en) | 1996-07-03 |
CN1079688C CN1079688C (en) | 2002-02-27 |
Family
ID=10750402
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN95190224A Expired - Fee Related CN1079688C (en) | 1994-02-15 | 1995-02-13 | The treatment of gaseous substances |
Country Status (9)
Country | Link |
---|---|
EP (1) | EP0693960A1 (en) |
JP (1) | JPH08509165A (en) |
KR (1) | KR960701686A (en) |
CN (1) | CN1079688C (en) |
AU (1) | AU1587295A (en) |
CA (1) | CA2160484A1 (en) |
GB (1) | GB9402886D0 (en) |
WO (1) | WO1995021682A1 (en) |
ZA (1) | ZA951226B (en) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE19603837C2 (en) * | 1996-02-05 | 2002-06-13 | Rag Ag | Process for H2S deposition from a gas containing H2S, e.g. B. coke oven gas, and device for performing the method |
EP0946261B1 (en) * | 1996-12-09 | 2001-09-19 | Imperial Chemical Industries Plc | Process for removing chlorine from gas stream |
CN107149856A (en) * | 2017-05-27 | 2017-09-12 | 佛山市三水万瑞达环保科技有限公司 | A kind of gas cleaning plant |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2940099A1 (en) * | 1979-10-03 | 1981-04-16 | VEB Chemieanlagenbaukombinat Leipzig-Grimma, DDR 7240 Grimma | Purificn. of waste gases via row of scrubbing towers - where washing liq. flows in countercurrent to the gas for efficient removal of noxious impurities |
FR2504024A1 (en) * | 1981-04-17 | 1982-10-22 | Steuler Industriewerke Gmbh | Toxic air components sepn. - by fibre mat filters sprayed with absorption agent |
DE3439165A1 (en) * | 1984-10-25 | 1986-04-30 | Linde Ag, 6200 Wiesbaden | METHOD FOR WASHING OUT ACID GASES FROM GAS MIXTURES |
DE4027404A1 (en) * | 1990-02-26 | 1991-08-29 | Fritz Curtius | Nitric oxide oxidn. in gas stream by scrubbing with nitric acid - contg. nitrous acid by desorbing of acid cpds. into gas and replacing nitrous acid |
DE4008099A1 (en) * | 1990-03-14 | 1991-09-19 | Metallgesellschaft Ag | Purificn. of effluent gas from rubbish combustion - contg. fly ash, heavy metal, acid gases etc. by spray adsorption and washing and moistening residue with used washing liq. |
EP0487834A1 (en) * | 1990-08-30 | 1992-06-03 | Fritz Curtius | Oxidative washing process for cleaning waste gases |
-
1994
- 1994-02-15 GB GB9402886A patent/GB9402886D0/en active Pending
-
1995
- 1995-02-13 CN CN95190224A patent/CN1079688C/en not_active Expired - Fee Related
- 1995-02-13 KR KR1019950704503A patent/KR960701686A/en not_active Application Discontinuation
- 1995-02-13 AU AU15872/95A patent/AU1587295A/en not_active Abandoned
- 1995-02-13 JP JP7521070A patent/JPH08509165A/en active Pending
- 1995-02-13 WO PCT/GB1995/000284 patent/WO1995021682A1/en not_active Application Discontinuation
- 1995-02-13 CA CA002160484A patent/CA2160484A1/en not_active Abandoned
- 1995-02-13 EP EP95907783A patent/EP0693960A1/en not_active Withdrawn
- 1995-02-15 ZA ZA951226A patent/ZA951226B/en unknown
Also Published As
Publication number | Publication date |
---|---|
CN1079688C (en) | 2002-02-27 |
WO1995021682A1 (en) | 1995-08-17 |
GB9402886D0 (en) | 1994-04-06 |
ZA951226B (en) | 1995-10-18 |
KR960701686A (en) | 1996-03-28 |
CA2160484A1 (en) | 1995-08-17 |
JPH08509165A (en) | 1996-10-01 |
EP0693960A1 (en) | 1996-01-31 |
AU1587295A (en) | 1995-08-29 |
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