EP0007850A1 - Plant for recovering energy - Google Patents
Plant for recovering energy Download PDFInfo
- Publication number
- EP0007850A1 EP0007850A1 EP79400491A EP79400491A EP0007850A1 EP 0007850 A1 EP0007850 A1 EP 0007850A1 EP 79400491 A EP79400491 A EP 79400491A EP 79400491 A EP79400491 A EP 79400491A EP 0007850 A1 EP0007850 A1 EP 0007850A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- condenser
- exchanger
- series
- evaporator
- energy
- 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.)
- Withdrawn
Links
- 238000009434 installation Methods 0.000 claims abstract description 11
- 238000011084 recovery Methods 0.000 claims abstract description 10
- 239000012530 fluid Substances 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 6
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 4
- NPPQSCRMBWNHMW-UHFFFAOYSA-N Meprobamate Chemical compound NC(=O)OCC(C)(CCC)COC(N)=O NPPQSCRMBWNHMW-UHFFFAOYSA-N 0.000 claims 1
- 238000001816 cooling Methods 0.000 abstract description 7
- 238000001704 evaporation Methods 0.000 abstract description 4
- 230000008020 evaporation Effects 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 10
- 229910021529 ammonia Inorganic materials 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 3
- 229910052770 Uranium Inorganic materials 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000005372 isotope separation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- SANRKQGLYCLAFE-UHFFFAOYSA-H uranium hexafluoride Chemical compound F[U](F)(F)(F)(F)F SANRKQGLYCLAFE-UHFFFAOYSA-H 0.000 description 2
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
- F01K3/18—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
- F01K3/185—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters using waste heat from outside the plant
Definitions
- the present invention relates to energy recovery installations, in particular to installations aiming to recover energy originating from low-temperature heat, for example from an isotopic separation plant. uranium and transfer this recovered energy into electrical energy.
- Isotopic separation of uranium is currently carried out by passing part of the flow of uranium hexafluoride through porous barriers called diffusers.
- This operation requires pressurization, carried out using compressors which compress the uranium hexafluoride before directing it towards the diffusers.
- These compressors require cooling by circulation of water, the temperature of which is raised, at the outlet of the cooling circuit, to relatively low values, of the order of 90 to 120 ° C. in general.
- This cooling water is sent to an exchanger from which it leaves at a lower temperature, adjusted for its reuse, the energy coming from this cooling can then be recovered thanks to the exchanger and supply for example a turbine connected to an alternator. .
- the present invention relates to an energy recovery installation at low temperature with a higher efficiency than that of installations known hitherto.
- the installation of the invention is of the type with two loops each comprising an exchanger-evaporator, at least one expansion turbine providing external work, and a condenser, installation in which the two exchanger-evaporators are traversed in series by the liquid.
- the two loops use identical fluids working at different pressures and temperatures in each loop, each downstream evaporator or condenser being adjusted to a pressure and temperature lower than that of the upstream evaporator or condenser, considered in the direction of circulation of the hot liquid or the coolant.
- references 1 and 2 designate two conventional exchangers operating by evaporation of an auxiliary fluid, such as ammonia taken from the same tank 25.
- the amonl exchanger has an upper inlet 3 of water from the circuit for cooling the compressors of the separation plant, and a lower outlet 4 for water cooled to a determined temperature T 1 .
- the downstream exchanger 2 has a water inlet 5 and a water outlet 6 at a determined temperature T 2 . Water enters in 3 at a relatively low temperature T 0 , of the order of 95 ° C. for example.
- the outlet 4 and the inlet 5 are connected to each other, the exchangers 1 and 2 therefore being supplied in series with the cooling water coming from the compressors.
- the water circulates in each of the exchangers 1 and 2 through a bundle of tubes 7 connecting two end plates 8, 9.
- the water outlet temperatures (T 1 , T 2 ) of each of the exchangers 1 and 2 are regulated by means of a temperature measuring device (respectively 10 and 11) acting on a regulating valve (respectively 12 and 13) of the evaporation fluid.
- Each of the upstream 1 or downstream 2 exchangers is part of an auxiliary fluid working loop comprising respectively a steam turbine 18 or 19, a condenser 20 or 21, a circulation pump 16 or 17 and a control valve 12 or 13
- Each of the loops is filled with the same ammonia fluid by means of feed pumps 23 or 24 from the same tank 25.
- the ammonia circulates, in a conventional manner, according to the following cycle:
- the ammonia issuing, in the liquid state, and at low temperature from the condenser 14, 15 is brought to a high pressure using a pump 16, 17 and introduced, through the regulating valve 12, 13 into the lower part of the exchanger 1, 2 in which it circulates between the heating tubes 7. It is thus heated, vaporized, then superheated, and feeds, at the outlet of the exchanger 1, 2 a steam turbine 18, 19 After its expansion in the turbine, the steam is sent to the condenser 14, 15 where it is brought back to the liquid state by the in through a cooling coil 20, 21 with water circulation.
- the water circulation cooling circuits 20, 21 of the two condensers 14, 15 are also arranged in series.
- the energy recovery circuit of the invention makes it possible to obtain a non-negligible increase in yield compared to the circuits known hitherto.
- the series connection of the water circulation circuits both in the exchangers and in the condensers makes it possible to obtain a more rational use of the steam produced and a reduction in the pumping power for the water supply to the condensers , so that the energy recovery gain is increased.
- the upstream exchanger 1 operates at an ammonia pressure higher than that under which the downstream exchanger operates.
- the intermediate temperature T 1 is advantageously chosen as being the median temperature between the inlet temperature T 0 corresponding to that of the water at the outlet of the compressors and the outlet temperature T 2 , the value of which is fixed either by optimization of the recovery system either by requirements from the separation plant.
- the pressure and temperature of the upstream condenser 14 are slightly higher than those of the downstream condenser 15, which allows an improvement in the distribution of the detents between the two machines, and which also makes it possible to obtain a less humid vapor at the exhaust. of the higher pressure turbine 18.
- the invention finds its use for energy recovery.
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
Description
tation d'énen présente invention se rapporte aux installations de récupé- rat on d'énergie, en particulier aux installations ayant pour but de récupérer l'énergie provenant de chaleurs à basse température issues par exemple d'une usine de séparation isotopique de l'uranium et de transor- mer cette énergie récupérée en énergie électrique.The present invention relates to energy recovery installations, in particular to installations aiming to recover energy originating from low-temperature heat, for example from an isotopic separation plant. uranium and transfer this recovered energy into electrical energy.
La séparation isotopique de l'uranium est actuellement réalisée en faisant passer une partie du flux d'hexafluorure d'uranium à travers des barrières poreuses appelées diffuseurs. Cette opération nécessite une mise en pression, effectuée à l'aide de compresseurs qui compriment l'hexafluorure d'uranium avant de le diriger vers les diffuseurs. Ces compresseurs nécessitent un refroidissement par circulation d'eau, dont la température se trouve relevée, en sortie de circuit de refroidissement, à des valeurs relativement basses, de l'ordre de 90 à 120°C en général. Cette eau de refroidissement est envoyée dans un échangeur d'où elle sort à une température inférieure, ajustée pour sa réutilisation, l'énergie provenant de ce refroidissement pouvant alors être récupérée grâce à l'échangeur et alimenter par exemple une turbine reliée à un alternateur.Isotopic separation of uranium is currently carried out by passing part of the flow of uranium hexafluoride through porous barriers called diffusers. This operation requires pressurization, carried out using compressors which compress the uranium hexafluoride before directing it towards the diffusers. These compressors require cooling by circulation of water, the temperature of which is raised, at the outlet of the cooling circuit, to relatively low values, of the order of 90 to 120 ° C. in general. This cooling water is sent to an exchanger from which it leaves at a lower temperature, adjusted for its reuse, the energy coming from this cooling can then be recovered thanks to the exchanger and supply for example a turbine connected to an alternator. .
En raison du faible niveau des températures mises en jeu, le rendement de la transformation est relativement faible avec les dispositifs de récupération utilisés actuellement.Due to the low level of temperatures involved, the transformation yield is relatively low with the recovery devices currently used.
La présente invention se rapporte à une installation de récupération d'énergie à basse température de rendement supérieur à celui des installations connues jusqu'alors. L'installation de l'invention est du type à deux boucles comportant chacune un échangeur-évaporateur, au moins une turbine de détente fournissant un travail extérieur, et un condenseur, installation dans laquelle les deux échangeurs-évaporateurs sont parcourus en série par le liquide chaud dont on veut récupérer l'énergie, et dans laquelle les deux condenseurs sont également parcourus en série par un liquide de refroidissement, Sion l'invention, les deux boucles utilisent des fluides identiques travaillant à des pressions et températures différentes dans chaque boucle, chaque évaporateur ou condenseur aval étant réglé à une pression et température inférieures à celles de l'évaporateur ou condenseur amont, considéré dans le sens de circulation du liquide chaud ou du liquide de refroidissement.The present invention relates to an energy recovery installation at low temperature with a higher efficiency than that of installations known hitherto. The installation of the invention is of the type with two loops each comprising an exchanger-evaporator, at least one expansion turbine providing external work, and a condenser, installation in which the two exchanger-evaporators are traversed in series by the liquid. hot whose energy we want to recover, and in which the two condensers are also traversed in series by a coolant, Sion the invention, the two loops use identical fluids working at different pressures and temperatures in each loop, each downstream evaporator or condenser being adjusted to a pressure and temperature lower than that of the upstream evaporator or condenser, considered in the direction of circulation of the hot liquid or the coolant.
L'invention sera mieux comprise à l'aide de la description suivante d'un exemple de réalisation, en référence à la figure unique annexée qui représente schématiquement une installation de récupération de chaleur à basse température conforme à l'invention.The invention will be better understood with the aid of the following description of an exemplary embodiment, with reference to the attached single figure which schematically represents a low temperature heat recovery installation according to the invention.
Sur la figure, les références 1 et 2 désignent deux échangeurs classiques fonctionnant par évaporation d'un fluide auxiliaire, tel que de l'ammoniaque prélevé sur un même réservoir 25. L'échangeur amonl possède une entrée supérieure 3 d'eau provenant du circuit de refroidissement des compresseurs de l'usine de séparation, et une sortie inférieure 4 d'eau refroidie à une température T1 déterminée. De même l'échangeur aval 2 possède une entrée d'eau 5 et une sortie d'eau 6 à une température T2 déterminée. L'eau entre en 3 à une température T0 relativement basse, de l'ordre de 95°C par exemple. Conformément à l'une des deux caractéristiques combinées de l'invention, la sortie 4 et l'entrée 5 sont reliées l'une à l'autre, les échangeurs 1 et 2 étant donc alimentés en série par l'eau de refroidissement provenant des compresseurs.In the figure,
De manière connue en soi, l'eau circule dans chacun des échangeurs 1 et 2 à travers un faisceau de tubes 7 reliant deux plaques d'extrémité 8, 9. De manière classique également, les températures de sortie d'eau (T1, T2) de chacun des échangeurs 1 et 2 sont réglées par l'intermédiaire d'un appareil de mesure de température (respectivement 10 et 11) agissant sur une vanne de régulation (respectivement 12 et 13) du fluide d'évaporation.In a manner known per se, the water circulates in each of the
Chacun des échangeurs amont 1 ou aval 2 fait partie d'une boucle de travail du fluide auxiliaire comportant respectivement une turbine à vapeur 18 ou 19, un condenseur 20 ou 21, une pompe de circulation 16 ou 17 et une vanne de régulation 12 ou 13. Chacune des boucles est remplie par un même fluide ammoniaque au moyen des pompes d'alimentation 23 ou 24 à partir du même réservoir 25. Dans chaque boucle l'ammoniaque circule, de manière classique, suivant le cycle suivant :Each of the upstream 1 or downstream 2 exchangers is part of an auxiliary fluid working loop comprising respectively a
L'ammoniaque issu, à l'état liquide, et à basse température du condenseur 14, 15 est amené à une pression élevée à l'aide d'une pompe 16, 17 et introduit, à travers la vanne de régulation 12, 13 dans la partie basse de l'échangeur 1, 2 dans lequel il circule entre les tubes de réchauffage 7. Il est ainsi réchauffé, vaporisé, puis surchauffé, et alimente, en sortie de l'échangeur 1, 2 une turbine à vapeur 18, 19. Après sa détente dans la turbine, la vapeur est envoyée dans le condenseur 14, 15 où elle est ramenée à l'état liquide par l'intermédiaire d'un serpentin de refroidissement 20, 21 à circulation d'eau. Conforméme à la seconde caractéristique combinée de l'invention, les circuits de refroidissement par circulation d'eau 20, 21 des deux condenseurs 14, 15 sont également disposés en série.The ammonia issuing, in the liquid state, and at low temperature from the
Le circuit de récupération d'énergie de l'invention permet d'obtenir une augmentation de rendement non négligeable par rapport aux circuits connus jusqu'alors. La mise en série des circuits de circulation d'eau aussi bien dans les échangeurs que dans les condenseurs permet en effet d'obtenir une utilisation plus rationnelle de la vapeur produite et une diminution de la puissance de pompage pour l'alimentation en eau des condenseurs, de sorte que le gain de récupération d'énergie s'en trouve augmenté. L'échangeur amont 1 fonctionne à une pression d'ammoniaque supérieure à celle sous laquelle fonctionne l'échangeur aval. La température intermédiaire T1 est avantageusement choisie comme étant la température médiane entre la température d'entrée T0 correspondant à celle de l'eau à la sortie des compresseurs et la température de sortie T2 dont la valeur est fixée soit par l'optimisation du dispositif de récupération soit par des impératifs provenant de l'usine de séparation. Les pression et température du condenseur amont 14 sont légèrement supérieures à celles du condenseur aval 15, ce qui permet une amélioration de la répartition des détentes entre les deux machines, et ce qui .permet également d'obtenir une vapeur moins humide à l'échappement de la turbine 18 à plus haute pression.The energy recovery circuit of the invention makes it possible to obtain a non-negligible increase in yield compared to the circuits known hitherto. The series connection of the water circulation circuits both in the exchangers and in the condensers makes it possible to obtain a more rational use of the steam produced and a reduction in the pumping power for the water supply to the condensers , so that the energy recovery gain is increased. The upstream exchanger 1 operates at an ammonia pressure higher than that under which the downstream exchanger operates. The intermediate temperature T 1 is advantageously chosen as being the median temperature between the inlet temperature T 0 corresponding to that of the water at the outlet of the compressors and the outlet temperature T 2 , the value of which is fixed either by optimization of the recovery system either by requirements from the separation plant. The pressure and temperature of the
L'invention trouve son utilisation pour la récupération d'énergie.The invention finds its use for energy recovery.
Claims (1)
installation dans laquelle les deux échangeurs-évaporateurs sont parcou- rus en série par le liquide chaud dont on veut récupérer l'énergie, et dans laquelle les deux condenseurs sont également parcourus en séril par un liquide de refroidissement,
caractérisé par le fait que les deux boucles utilisent des fluides identiques travaillant à des pressions et températures différentes dans chaque boucle, chaque évaporateur ou condenseur aval étant réglé à une pression et température inférieures à celle de l'évaporateur ou condenseur amont, considéré dans le sens de circulation du liquide chaud ou du liquide de refroidissement.Energy recovery installation with two loops each comprising an exchanger-evaporator, at least one expansion turbine providing external work, and a condenser,
installation in which the two evaporators-exchangers are traversed in series by the hot liquid which one wants to recover energy, and wherein the two condensers are also covered in Seril by a coolant,
characterized by the fact that the two loops use identical fluids working at different pressures and temperatures in each loop, each downstream evaporator or condenser being adjusted to a pressure and temperature lower than that of the upstream evaporator or condenser, considered in the direction circulation of hot liquid or coolant.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR7820956 | 1978-07-13 | ||
| FR7820956A FR2431025A1 (en) | 1978-07-13 | 1978-07-13 | ENERGY RECOVERY PLANT |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| EP0007850A1 true EP0007850A1 (en) | 1980-02-06 |
Family
ID=9210724
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP79400491A Withdrawn EP0007850A1 (en) | 1978-07-13 | 1979-07-11 | Plant for recovering energy |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0007850A1 (en) |
| JP (1) | JPS5519985A (en) |
| BE (1) | BE877702A (en) |
| FR (1) | FR2431025A1 (en) |
| IT (1) | IT1119039B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4329919A (en) * | 1978-11-13 | 1982-05-18 | Andersen Ariel A | Time-energy conserving low cost home pressure cooking system |
| CN102536363A (en) * | 2010-11-19 | 2012-07-04 | 通用电气公司 | Rankine cycle integrated with organic rankine cycle and absorption chiller cycle |
| WO2010016825A3 (en) * | 2008-08-04 | 2013-01-03 | United Technologies Corporation | Cascaded condenser for multi-unit geothermal orc |
| US10830217B2 (en) | 2017-03-24 | 2020-11-10 | Ihi Corporation | Binary power generation system |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61149507A (en) * | 1984-12-24 | 1986-07-08 | Hisaka Works Ltd | Heat recovery device |
| JP4808006B2 (en) * | 2005-11-04 | 2011-11-02 | 株式会社荏原製作所 | Drive system |
| JP5862133B2 (en) | 2011-09-09 | 2016-02-16 | 国立大学法人佐賀大学 | Steam power cycle system |
| JP5843391B2 (en) * | 2011-12-14 | 2016-01-13 | 株式会社タクマ | Waste power generation system |
| JP7328101B2 (en) * | 2019-09-25 | 2023-08-16 | メタウォーター株式会社 | cogeneration system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CH239086A (en) * | 1939-04-15 | 1945-09-15 | D Amelio Luigi | Process for the use of heat contained in hot water for the purpose of producing mechanical energy. |
| CH251501A (en) * | 1946-06-04 | 1947-10-31 | Skoda Kp | Process and facility for waste heat recovery. |
| FR1128733A (en) * | 1955-07-09 | 1957-01-09 | Francoise Des Const Babcock & | Heat recovery from gas masses |
| GB1137484A (en) * | 1964-12-30 | 1968-12-18 | Power Gas Ltd | Improvements in or relating to the recovery of waste heat in the form of mechanical energy |
| US3795103A (en) * | 1971-09-30 | 1974-03-05 | J Anderson | Dual fluid cycle |
-
1978
- 1978-07-13 FR FR7820956A patent/FR2431025A1/en active Granted
-
1979
- 1979-07-11 EP EP79400491A patent/EP0007850A1/en not_active Withdrawn
- 1979-07-13 JP JP8920479A patent/JPS5519985A/en active Pending
- 1979-07-13 BE BE0/196302A patent/BE877702A/en not_active IP Right Cessation
- 1979-07-13 IT IT68471/79A patent/IT1119039B/en active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CH239086A (en) * | 1939-04-15 | 1945-09-15 | D Amelio Luigi | Process for the use of heat contained in hot water for the purpose of producing mechanical energy. |
| CH251501A (en) * | 1946-06-04 | 1947-10-31 | Skoda Kp | Process and facility for waste heat recovery. |
| FR1128733A (en) * | 1955-07-09 | 1957-01-09 | Francoise Des Const Babcock & | Heat recovery from gas masses |
| GB1137484A (en) * | 1964-12-30 | 1968-12-18 | Power Gas Ltd | Improvements in or relating to the recovery of waste heat in the form of mechanical energy |
| US3795103A (en) * | 1971-09-30 | 1974-03-05 | J Anderson | Dual fluid cycle |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4329919A (en) * | 1978-11-13 | 1982-05-18 | Andersen Ariel A | Time-energy conserving low cost home pressure cooking system |
| WO2010016825A3 (en) * | 2008-08-04 | 2013-01-03 | United Technologies Corporation | Cascaded condenser for multi-unit geothermal orc |
| CN102536363A (en) * | 2010-11-19 | 2012-07-04 | 通用电气公司 | Rankine cycle integrated with organic rankine cycle and absorption chiller cycle |
| EP2455591A3 (en) * | 2010-11-19 | 2014-02-19 | General Electric Company | Rankine cycle integrated with organic rankine cycle and absorption chiller cycle |
| US8904791B2 (en) | 2010-11-19 | 2014-12-09 | General Electric Company | Rankine cycle integrated with organic rankine cycle and absorption chiller cycle |
| CN102536363B (en) * | 2010-11-19 | 2015-05-20 | 通用电气公司 | Rankine cycle integrated with organic rankine cycle and absorption chiller cycle |
| US10830217B2 (en) | 2017-03-24 | 2020-11-10 | Ihi Corporation | Binary power generation system |
Also Published As
| Publication number | Publication date |
|---|---|
| FR2431025A1 (en) | 1980-02-08 |
| FR2431025B1 (en) | 1982-03-19 |
| BE877702A (en) | 1980-01-14 |
| IT1119039B (en) | 1986-03-03 |
| JPS5519985A (en) | 1980-02-13 |
| IT7968471A0 (en) | 1979-07-13 |
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| PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
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| AK | Designated contracting states |
Designated state(s): DE GB NL |
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| 17P | Request for examination filed | ||
| STAA | Information on the status of an ep patent application or granted ep patent |
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| 18W | Application withdrawn |
Withdrawal date: 19810102 |
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| RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: TILLEQUIN, JEAN |