EP2379968A1 - Procede de capture du dioxyde de carbone par cryo-condensation - Google Patents
Procede de capture du dioxyde de carbone par cryo-condensationInfo
- Publication number
- EP2379968A1 EP2379968A1 EP09803847A EP09803847A EP2379968A1 EP 2379968 A1 EP2379968 A1 EP 2379968A1 EP 09803847 A EP09803847 A EP 09803847A EP 09803847 A EP09803847 A EP 09803847A EP 2379968 A1 EP2379968 A1 EP 2379968A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- fluid
- rich
- liquid
- treated
- heat exchange
- 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- Withdrawn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
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
- B01D53/002—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 condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
Definitions
- the present invention relates to a process for capturing carbon dioxide in a fluid comprising at least one more volatile compound than CO2 carbon dioxide, for example methane CH4, oxygen O2, argon Ar, nitrogen N2, carbon monoxide CO, helium He and / or hydrogen H2.
- the invention can be applied in particular to electricity production units and / or steam from carbonaceous fuels such as coal, hydrocarbons (natural gas, fuel, petroleum residues ...), household waste, biomass but also to gases from refineries, chemical factories, steel factories or cement factories, to the processing of natural gas at the output of production wells. It could also apply to the fumes of boilers used for heating buildings or even the exhaust of transport vehicles, more generally to any industrial process generating fumes including CO2.
- Carbon dioxide is a greenhouse gas. For environmental and / or economic reasons, it is increasingly desirable to reduce or even eliminate CO 2 emissions into the atmosphere, by capturing it and then, for example, storing it in appropriate geological layers or enhancing it. as a product.
- the document FR-A-2894838 discloses the same type of process, with a recycling of a portion of the liquid CO2 produced. Part of the CO2-poor gas produced is used to condense the water in the mixture to be treated. Cold can be provided by the vaporization of LNG (liquefied natural gas). This synergy reduces the specific energy consumption of the process, which nevertheless remains high, and requires an LNG terminal.
- LNG liquefied natural gas
- An object of the present invention is to provide an improved method of capturing carbon dioxide from a fluid comprising CO2 and at least one more volatile compound than this.
- the invention firstly relates to a process for producing at least one CO2-poor gas and one or more CO2-rich primary fluids from a process fluid comprising CO2 and at least one more volatile compound.
- the CO2 implementing: a) a first cooling of said fluid to be treated by heat exchange without change of state; b) a second cooling of at least a portion of said coolant to be treated cooled in step a) so as to obtain at least one solid comprising predominantly CO2 and at least said CO2-poor gas; and c) a step comprising liquefying at least a portion of said solid and making it possible to obtain said one or more primary fluids rich in
- step a) characterized in that at least a portion of said first cooling performed in step a) is obtained by heating at least a portion of said one or more CO2-rich primary fluids.
- the fluid to be treated generally comes from a boiler or any installation producing smoke. These fumes may have undergone several pre-treatments, in particular to remove NOx (nitrogen oxides), dust, SOx (sulfur oxides) and / or water.
- NOx nitrogen oxides
- SOx sulfur oxides
- the fluid to be treated is either monophasic, in gaseous or liquid form, or multiphase.
- gaseous form is meant “essentially gaseous”. Indeed, if the fluid to be treated consists of fumes pretreated, it may contain especially dust, solid particles such as soot and / or droplets of liquid.
- the fluid to be treated contains CO2 which it is desired to separate by cryo- condensation from the other constituents of said fluid.
- These other constituents comprise at least one or more compounds which are more volatile than carbon dioxide in the sense of condensation, for example methane CH4, oxygen O2, argon Ar, nitrogen N2, carbon monoxide CO, Helium He and / or hydrogen
- the fluids to be treated generally comprise mainly nitrogen, or mainly CO or predominantly hydrogen.
- step a) the fluid to be treated is first cooled without changing state.
- the inventors have shown that this cooling can advantageously be done at least partly by heat exchange with fluids rich in CO2 from the separation process.
- it can advantageously be done at least partly by heat exchange with the CO2-poor gas resulting from the separation process.
- Step b) consists in solidifying initially gaseous CO2 by bringing the fluid to be treated to a temperature below the triple point of CO2, whereas the partial pressure of the CO2 in the fluid to be treated is lower than that of the triple point of CO2. .
- the total pressure of the fluid to be treated is close to atmospheric pressure. This solidification operation is sometimes called “cryo-condensation” or “anti-sublimation” of CO2 and by extension of the fluid to be treated.
- CO2-poor gas that is to say comprising less than 50% of CO2 by volume and preferably less than 10% CO2 by volume.
- said CO2-poor gas comprises more than 1% of CO2 by volume.
- it comprises more than 2%.
- it comprises more than 5%.
- a solid is formed comprising predominantly CO2, ie at least 90% by volume brought back to the gaseous state, preferably at least 95% by volume and even more preferably at least 99% of CO2 by volume. This solid may comprise other compounds than CO2.
- solid may not be purely constituted of solid CO2.
- This "solid” may comprise non-solid parts such as fluid inclusions (drops, bubbles, etc.).
- This solid is then isolated from the non-solidified compounds after cryo- condensation and recovered. Then, in step c), it is brought back to conditions of temperature and pressure such that it changes to a fluid, liquid and / or gaseous state. It can therefore occur liquefaction of at least a portion of said solid. This gives rise to one or more primary fluids rich in CO2. These fluids are said to be “primary” to distinguish them from process fluids that are called “secondary” fluids. By “rich in CO2” is meant “comprising predominantly CO2" in the sense defined above.
- the inventors have shown that it is advantageous to carry out at least a part of the first cooling of the fluid to be treated by exchanging heat with the primary fluids rich in CO2.
- the advantage is to recover their content in cold and reduce the need for external frigories, usually provided by one or more refrigerating cycles. This supposes to vaporize a part of said primary fluids rich in CO2 and entails an additional cost in the compression made for the transport and / or injection into the subsoil of said fluids rich in CO2.
- the method according to the invention may comprise one or more of the following characteristics:
- said step b) takes place at a total pressure such that the partial pressure of the CO2 contained in said fluid to be treated is less than or equal to that of the triple point of the CO2, said total pressure preferably being close to atmospheric pressure.
- step c) takes place at a total pressure greater than that of the triple point of CO2, preferably close to it.
- step c) comprises a liquefaction obtained by introducing at least a portion of said solid into a liquid bath comprising predominantly CO2 and an extraction of said liquid bath of at least one primary liquid rich in CO2.
- said liquid bath is heated in one or more of the following ways:
- At least a portion of said CO2-rich primary fluids is obtained from said CO2-rich primary liquid in one or more of the following ways:
- At least part of said CO2-rich primary fluids comprises a liquid phase and said heating of at least a portion of said CO2-rich primary fluids by heat exchange with said fluid to be treated vaporises at least a part of this liquid phase.
- At least one of said primary fluids rich in CO2 remains in the liquid or pseudo-liquid state during said heating of at least a portion of said primary fluids rich in CO2 by heat exchange with said fluid to be treated.
- the pseudo-liquid state is defined by a partial pressure of CO2 higher than the critical pressure and a temperature between the solidification temperature and the temperature of the critical point.
- at least a part of said first cooling carried out in step a) is obtained by heat exchange with an intermediate fluid having exchanged cold with at least a portion of said one or more primary fluids rich in CO2.
- the "liquid bath” referred to above may be contained in a container. It is generally at a temperature between -50 ° C. and the temperature of the tripe point of CO2 (-56.6 ° C.), preferably between -55 ° C. and -56.6 ° C. It is mainly composed of liquid CO2, resulting from the melting of said solid obtained by cryo-condensation. The total pressure prevailing above the liquid bath is greater than or equal to that of the triple point of CO2, preferably close to it. From this bath is extracted, by any appropriate means, a primary liquid rich in CO2.
- the solid which is poured into this liquid bath is at a temperature lower than that of the bath, it is therefore necessary to heat the bath to maintain its temperature and ensure the melting of said solid.
- This heating can be carried out in several ways, by heat exchange with one or more other fluids, usually by indirect contact, without mixing.
- the heat exchange can be carried out by direct contact by introducing one or more fluids rich in CO2 at a temperature greater than that of the bath in the liquid bath.
- This direct contact heat exchange is generally more efficient than indirect exchange.
- a fluid rich in CO2 slightly warmer than the liquid bath is then sufficient. This limits the irreversibilities and increases the efficiency of the process.
- the fluid that heats the liquid bath by indirect exchange is itself cooled. It can therefore be used to cool the fluid to be treated. In this way, the cold brought to the liquid bath by the solid resulting from the cryo-condensation can be at least partly recovered elsewhere in the process, in particular for the first cooling of the fluid to be treated. As a result, overall efficiency is improved.
- several fluids rich in CO2 are produced at different pressures. This makes it possible to finely adjust the amount of heat transferred and the energy required to recompress the CO2-rich primary fluids after the exchange. Low pressures and vaporization of CO2-rich fluids favor the recovery of frigories, but involve a higher compression cost for these products.
- the heat exchange between the fluids rich in CO2 and the fluid to be treated can be via one or more intermediate fluids, ie the fluids rich in CO2 will yield part of their cold to intermediate fluid, which will then give some of this cold to the fluid to be treated.
- the invention also relates to the process applied to industrial fumes for the purpose of capturing CO2.
- these fumes come from an energy production plant (steam, electricity) and may have undergone pre-treatments.
- FIG. 1 schematically represents a CO2 capture unit implementing a method according to the invention
- FIG. 2 shows schematically the use of a method according to the invention in a coal-based power generation facility.
- FIG. 1 implements the steps described below.
- the fluid 24 consisting of flue gas is compressed in a compressor 101, in particular to compensate for the pressure losses on the various equipment of the unit. Note that this compression can be combined with the so-called draw compression of the boiler giving rise to smoke. It can also be carried out between other stages of the process, or downstream of the CO2 separation process; the compressed fluid 30 is injected into a filter 103 to remove the particles to a concentration level of less than 1 mg / m 3 , preferably less than 100 ⁇ g / m 3 ;
- the dust-free fluid 32 is cooled to a temperature close to 0 0 C, generally between 0 0 C and 10 0 C, so as to condense the water vapor that it contains.
- This cooling is performed in a tower 105, with two-level water injection, cold water 36 and water at a temperature close to ambient 34. It is also possible to envisage indirect contact.
- the tower 105 may or may not have packings; the fluid 38 is sent to a residual water vapor removal unit 107, using for example one and / or the other of the following processes
- the adsorbent may be activated alumina, silica gel or a molecular sieve (3A, 4A, 5A, 13X, ...); o condensation in a direct or indirect contact exchanger.
- the dried fluid 40 is then introduced into the exchanger 109 where the fluid is cooled to a close temperature, but in any case, greater than the solidification temperature of the CO2.
- This can be determined by those skilled in the art knowing the pressure and the composition of the fluid 40 to be treated. The latter is located around -100 ° C if the CO2 content of the fluid to be treated is of the order of 15% by volume and for a pressure close to atmospheric pressure.
- the fluid 42 having undergone first cooling 109 is then introduced into an enclosure 111 to continue cooling to the temperature which ensures the desired capture rate of CO2.
- a cryo-condensation of at least a portion of the CO2 contained in the fluid 42 occurs, so as to produce on the one hand a gas 44 depleted of CO2 and on the other hand a solid 62 comprising mainly CO2.
- the gas 44 leaves the chamber 111 at a temperature of the order of -120 ° C. This temperature is chosen according to the target CO2 capture rate. With this temperature, the CO2 content in the gas 44 is of the order of 1.5% by volume, ie a capture rate of 90% starting from a fluid to be treated comprising 15% CO 2.
- this enclosure 111 a continuous solid cryo-condensation exchanger in which solid CO 2 is produced in the form of dry ice, which is extracted for example by a screw and pressurized for cooling. 'introduce in a bath of liquid CO2 121, where there is a pressure greater than that of the triple point of CO2. This pressurization can also be performed in batches in a silo system.
- Continuous solid cryo-condensation can itself be carried out in several ways:
- scraped surface exchanger the scrapers being for example screw-shaped so as to promote the extraction of the solid
- Fluidized bed exchanger so as to cause the dry ice and clean the tubes by particles for example of density higher than that of the dry ice
- the fluid 46 is then reheated in the exchanger 109.
- the fluid 48 may also be used in particular to regenerate the residual vapor elimination unit (107) and / or to produce cold water (115) by evaporation in a tower with direct contact 115 where a dry fluid 50 is introduced which will saturate with water by vaporizing a part;
- this bath 121 must be heated to remain liquid, to compensate for the cold input by the solid 62 (latent heat of fusion and sensible heat). This can be done in different ways: o by heat exchange with a hotter fluid 72, or by direct exchange, for example by taking a fluid 80 from the bath 121, by heating it in the exchanger 109 and re-injecting it into the bath 121; - The liquid 64 comprising predominantly CO2 is taken from the bath 121.
- this liquid is divided into three streams.
- the first is obtained by an expansion 65 to 5.5 bar absolute producing a two-phase fluid, gas-liquid 66.
- the second, 68 is obtained by compression 67, for example at 10 bar.
- the third, 70 is compressed for example at 55 bar.
- the 5.5 bar level brings cold to a temperature close to that of the triple point of CO2.
- the levels at 10 bar allows the transfer of the latent heat of vaporization of the fluid 68 to about -40 ° C.
- the fluid 70 does not vaporize during the exchange 109. This allows a good valuation of the frigories contained in the fluid 64 during the exchange 109 while limiting the energy required to produce a stream of purified and compressed CO2 5;
- the primary fluids 66, 68, 70 are compressed to a pressure level higher than the critical pressure of the CO2 thanks to the compressors 131, 132, 133.
- FIG. 2 represents a coal-based electricity generation installation, implementing various purification units 4, 5, 6 and 7 of the fumes 19.
- a primary air flow 15 passes through the unit 3 where the coal 15 is sprayed and driven to the burners of the boiler 1.
- a secondary air flow 16 is supplied directly to the burners to provide additional oxygen. necessary for an almost complete combustion of coal.
- Supply water 17 is sent to the boiler 1 to produce steam 18 which is expanded in a turbine 8.
- Unit 4 removes NOx for example by catalysis in the presence of ammonia.
- Unit 5 removes dust for example by electrostatic filter and unit 6 is a desulfurization system for removing SO2 and / or SO3.
- Units 4 and 6 may be redundant depending on the composition of the required product.
- the purified flow 24 from unit 6 (or 5 if 6 is not present) is sent to a low temperature purification unit 7 by cryoponding to produce a relatively pure CO2 flow rate and a residual flow rate. enriched in nitrogen.
- This unit 7 is also called a CO2 capture unit and implements a method according to the invention, as illustrated, for example, by FIG.
- the main advantages of the invention are therefore: to reduce the energy consumption of CO2 separation and compression, to give the possibility to adapt to different operating constraints, in particular the pressure at which CO2 must be obtained, the availability and the cost of the necessary frigories at separation by cryo-condensation.
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)
- Carbon And Carbon Compounds (AREA)
- Treating Waste Gases (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0858872A FR2940414B1 (fr) | 2008-12-19 | 2008-12-19 | Procede de capture du dioxyde de carbone par cryo-condensation |
PCT/FR2009/052505 WO2010076463A1 (fr) | 2008-12-19 | 2009-12-14 | Procede de capture du dioxyde de carbone par cryo-condensation |
Publications (1)
Publication Number | Publication Date |
---|---|
EP2379968A1 true EP2379968A1 (fr) | 2011-10-26 |
Family
ID=40942523
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP09803847A Withdrawn EP2379968A1 (fr) | 2008-12-19 | 2009-12-14 | Procede de capture du dioxyde de carbone par cryo-condensation |
Country Status (5)
Country | Link |
---|---|
US (1) | US20110252828A1 (fr) |
EP (1) | EP2379968A1 (fr) |
CN (1) | CN102257342B (fr) |
FR (1) | FR2940414B1 (fr) |
WO (1) | WO2010076463A1 (fr) |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8617292B2 (en) | 2009-12-15 | 2013-12-31 | L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Method of obtaining carbon dioxide from carbon dioxide-containing gas mixture |
US8764885B2 (en) | 2010-11-19 | 2014-07-01 | Sustainable Energy Solutions, Llc | Systems and methods for separating condensable vapors from gases by direct-contact heat exchange |
AU2012258510B2 (en) | 2011-05-26 | 2016-09-22 | Sustainable Energy Solutions, Llc | Systems and methods for separating condensable vapors from light gases or liquids by recuperative cryogenic processes |
US10066884B2 (en) | 2013-07-25 | 2018-09-04 | Denbury Resources Inc. | Method and apparatus for dampening flow variations and pressurizing carbon dioxide |
CN105545390A (zh) * | 2016-01-25 | 2016-05-04 | 辽宁石油化工大学 | 一种lng冷能梯级利用方法 |
US20190170441A1 (en) * | 2017-12-05 | 2019-06-06 | Larry Baxter | Pressure-Regulated Melting of Solids with Warm Fluids |
US20190170440A1 (en) * | 2017-12-05 | 2019-06-06 | Larry Baxter | Pressure-Regulated Melting of Solids |
CN108956232B (zh) * | 2018-08-03 | 2021-03-30 | 中国核动力研究设计院 | 一种生物样中碳-14的制样方法及制样设备 |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3614872A (en) * | 1967-12-22 | 1971-10-26 | Texaco Inc | Synthesis gas separation process |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB997507A (en) * | 1963-11-04 | 1965-07-07 | Couch Internat Methane Ltd | Process for the cold separation of gas mixtures |
TW366409B (en) * | 1997-07-01 | 1999-08-11 | Exxon Production Research Co | Process for liquefying a natural gas stream containing at least one freezable component |
CA2294742C (fr) * | 1997-07-01 | 2005-04-05 | Exxon Production Research Company | Procede de separation pour flux gazeux ayant des constituants multiples, dont au moins un constituant gelable |
FR2820052B1 (fr) * | 2001-01-30 | 2003-11-28 | Armines Ass Pour La Rech Et Le | Procede d'extraction du dioxyde de carbone par anti-sublimation en vue de son stockage |
US7219512B1 (en) * | 2001-05-04 | 2007-05-22 | Battelle Energy Alliance, Llc | Apparatus for the liquefaction of natural gas and methods relating to same |
FR2894838B1 (fr) * | 2005-12-21 | 2008-03-14 | Gaz De France Sa | Procede et systeme de capture du dioxyde de carbone present dans des fumees |
-
2008
- 2008-12-19 FR FR0858872A patent/FR2940414B1/fr not_active Expired - Fee Related
-
2009
- 2009-12-14 EP EP09803847A patent/EP2379968A1/fr not_active Withdrawn
- 2009-12-14 WO PCT/FR2009/052505 patent/WO2010076463A1/fr active Application Filing
- 2009-12-14 US US13/133,852 patent/US20110252828A1/en not_active Abandoned
- 2009-12-14 CN CN200980151178.3A patent/CN102257342B/zh not_active Expired - Fee Related
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3614872A (en) * | 1967-12-22 | 1971-10-26 | Texaco Inc | Synthesis gas separation process |
Non-Patent Citations (1)
Title |
---|
See also references of WO2010076463A1 * |
Also Published As
Publication number | Publication date |
---|---|
WO2010076463A1 (fr) | 2010-07-08 |
FR2940414A1 (fr) | 2010-06-25 |
US20110252828A1 (en) | 2011-10-20 |
CN102257342A (zh) | 2011-11-23 |
FR2940414B1 (fr) | 2012-10-26 |
CN102257342B (zh) | 2014-07-16 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP2379971B1 (fr) | Procédé de capture du co2 et de production d'eau froide | |
EP2488278B1 (fr) | Procédé de production d'au moins un gaz pauvre en co2 et d'au moins un fluide riche en co2 | |
EP1869385B1 (fr) | Procede et installation integres d'adsorption et de separation cryogenique pour la production de co2 | |
EP2379968A1 (fr) | Procede de capture du dioxyde de carbone par cryo-condensation | |
AU745739B2 (en) | Autorefrigeration separation of carbon dioxide | |
EP3393621A1 (fr) | Procede de production de biomethane par epuration de biogaz issu d'installations de stockage de dechets non-dangereux (isdnd) et installation pour la mise en uvre du procede | |
US20150240717A1 (en) | Increasing Combustibility of Low BTU Natural Gas | |
US20220065161A1 (en) | Liquid natural gas processing with hydrogen production | |
CA3024382C (fr) | Procede de separation cryogenique d'un debit d'alimentation contenant du methane et des gaz de l'air, installation pour la production de bio methane par epuration de biogaz issus d'installations de stockage de dechets non-dangereux (isdnd) mettant en oeuvre le procede | |
FR2924951A1 (fr) | Procede de co- ou tri-generation avec mise en oeuvre d'une premiere et d'une seconde unites de capture de h2s et/ou du co2 fonctionnant en parallele. | |
FR3075659B1 (fr) | Procede de production d'un courant de gaz naturel a partir d'un courant de biogaz. | |
FR2872890A1 (fr) | Procede integre d'adsorption et de separation cryogenique pour la production de co2 et installation pour la mise en oeuvre du procede | |
FR2940412A1 (fr) | Procede de capture du dioxyde de carbone par cryo-condensation | |
WO2019122661A1 (fr) | Procédé de distillation d'un courant gazeux contenant de l'oxygène | |
FR2823449A1 (fr) | Procede d'elimination d'oxygene d'un gaz contenant du gaz carbonique | |
FR2859483A1 (fr) | Procede de fabrication de fonte avec utilisation des gaz du haut-fourneau pour la recuperation assistee du petrole | |
FR2889971A1 (fr) | Prcede de valorisation du gaz de depressurisation d'une unite vpsa co2 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
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 |
|
17P | Request for examination filed |
Effective date: 20110719 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR |
|
DAX | Request for extension of the european patent (deleted) | ||
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: EXAMINATION IS IN PROGRESS |
|
17Q | First examination report despatched |
Effective date: 20170208 |
|
GRAP | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOSNIGR1 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: GRANT OF PATENT IS INTENDED |
|
INTG | Intention to grant announced |
Effective date: 20170929 |
|
GRAS | Grant fee paid |
Free format text: ORIGINAL CODE: EPIDOSNIGR3 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
|
18D | Application deemed to be withdrawn |
Effective date: 20180210 |