EP3475219A1 - Procédé de fabrication d'hydrogène de schiste - Google Patents
Procédé de fabrication d'hydrogène de schisteInfo
- Publication number
- EP3475219A1 EP3475219A1 EP17733904.1A EP17733904A EP3475219A1 EP 3475219 A1 EP3475219 A1 EP 3475219A1 EP 17733904 A EP17733904 A EP 17733904A EP 3475219 A1 EP3475219 A1 EP 3475219A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- hydrogen
- gas
- shale
- oil
- shale gas
- 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- Withdrawn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
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 129
- 239000001257 hydrogen Substances 0.000 title claims abstract description 128
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 238000000034 method Methods 0.000 title claims abstract description 40
- 230000008569 process Effects 0.000 title claims abstract description 35
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 25
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 146
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 88
- 239000007789 gas Substances 0.000 claims abstract description 87
- 239000003345 natural gas Substances 0.000 claims abstract description 50
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 48
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 20
- 230000003647 oxidation Effects 0.000 claims abstract description 19
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 19
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000001301 oxygen Substances 0.000 claims abstract description 10
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 10
- 238000009826 distribution Methods 0.000 claims abstract description 9
- 239000003079 shale oil Substances 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 8
- 238000001193 catalytic steam reforming Methods 0.000 claims abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims description 51
- 239000003245 coal Substances 0.000 claims description 23
- 230000015572 biosynthetic process Effects 0.000 claims description 19
- 238000003786 synthesis reaction Methods 0.000 claims description 18
- 238000002485 combustion reaction Methods 0.000 claims description 13
- 239000003077 lignite Substances 0.000 claims description 13
- 239000000446 fuel Substances 0.000 claims description 11
- 238000002407 reforming Methods 0.000 claims description 9
- 238000002309 gasification Methods 0.000 claims description 8
- 238000005553 drilling Methods 0.000 claims description 7
- 238000002453 autothermal reforming Methods 0.000 claims description 6
- 239000003208 petroleum Substances 0.000 claims description 6
- 230000009466 transformation Effects 0.000 claims description 5
- 238000001833 catalytic reforming Methods 0.000 claims description 3
- 230000033228 biological regulation Effects 0.000 claims description 2
- 238000010924 continuous production Methods 0.000 claims description 2
- 230000008878 coupling Effects 0.000 claims description 2
- 238000010168 coupling process Methods 0.000 claims description 2
- 238000005859 coupling reaction Methods 0.000 claims description 2
- 238000009434 installation Methods 0.000 claims 1
- 239000005431 greenhouse gas Substances 0.000 abstract description 16
- 230000008859 change Effects 0.000 abstract description 2
- 230000003466 anti-cipated effect Effects 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 43
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 33
- 229910002091 carbon monoxide Inorganic materials 0.000 description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- 230000005611 electricity Effects 0.000 description 16
- 229910052799 carbon Inorganic materials 0.000 description 15
- 239000003921 oil Substances 0.000 description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 12
- 239000002803 fossil fuel Substances 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 229910052717 sulfur Inorganic materials 0.000 description 8
- 239000011593 sulfur Substances 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 7
- 238000010792 warming Methods 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- 238000011282 treatment Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 238000011161 development Methods 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000008246 gaseous mixture Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 230000007704 transition Effects 0.000 description 4
- 150000001412 amines Chemical class 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 150000001721 carbon Chemical group 0.000 description 3
- 239000003502 gasoline Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 238000010926 purge Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000000629 steam reforming Methods 0.000 description 3
- 241001465754 Metazoa Species 0.000 description 2
- 241000283868 Oryx Species 0.000 description 2
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000543 intermediate Substances 0.000 description 2
- 239000003350 kerosene Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000009919 sequestration Effects 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000003643 water by type Substances 0.000 description 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical class CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 1
- 101100269674 Mus musculus Alyref2 gene Proteins 0.000 description 1
- 241001147416 Ursus maritimus Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 125000004093 cyano group Chemical group *C#N 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 208000001848 dysentery Diseases 0.000 description 1
- -1 electricity Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- NRBNGHCYDWUVLC-UHFFFAOYSA-N mtep Chemical compound S1C(C)=NC(C#CC=2C=NC=CC=2)=C1 NRBNGHCYDWUVLC-UHFFFAOYSA-N 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 150000002828 nitro derivatives Chemical class 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 238000005038 synthesis gas manufacturing Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 230000029305 taxis Effects 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/295—Gasification of minerals, e.g. for producing mixtures of combustible gases
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0405—Purification by membrane separation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0415—Purification by absorption in liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
- C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/046—Purification by cryogenic separation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/066—Integration with other chemical processes with fuel cells
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
- C01B2203/0883—Methods of cooling by indirect heat exchange
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1247—Higher hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1258—Pre-treatment of the feed
- C01B2203/1264—Catalytic pre-treatment of the feed
- C01B2203/127—Catalytic desulfurisation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/84—Energy production
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/86—Carbon dioxide sequestration
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
Definitions
- the present invention relates to a process for producing shale hydrogen.
- shale hydrogen is obtained from shale gas or shale oil which is extracted by drilling, this shale gas (or oil) is then directly converted into hydrogen in a production unit of hydrogen by reforming or partial oxidation in which the carbon dioxide is extracted, then liquefied and is recycled in the borehole or it will be used to extract the gas (or oil) and in which it will finally be sequestered, the hydrogen obtained is used directly in a power plant located on the site and / or injected into a hydrogen distribution network built for this purpose.
- the shale hydrogen thus produced and distributed is the cheapest clean fuel on the market and its price is of the order of magnitude of the price of natural gas, ie € 25 / MWh, and this by amortizing investments with returns on investments 25%. If a carbon tax of € 50 per tonne is implemented, it becomes the cheapest fuel on the all energy market.
- This shale hydrogen achieves a reduction of three to four GHG emissions from a country like France and by 2040 is better than the European target and better than the desired objective at COP21.
- GigaHydrogen Plant or Giga Plant a unit whose power exceeds 2250MW (2.25GW) and typically 4500 MW (4.5GW).
- Hydraulic fracturing is a fairly old technique, several authors indicate the year 1949 as the date of the first fracturing, since millions of wells were drilled. In the United States some wells have posed environmental problems as a result of non-compliance with good operating practices. Hydraulic fracturing is done by injecting water or a pressurized gas that may be carbon dioxide, nitrogen, propane, petroleum-based fluids. Carbon dioxide is not hitherto used in view of its cost, the propane of its flammability.
- Carbon dioxide is known for its exceptional solvent properties when used at supercritical pressure, pressure above 72.9 bar.
- Hydrogen can be transported by hydrogen pipeline, the largest existing is exploited in the Ruhr by Hùls, its length is 210 km long, its low capacity of 1 billion m3 / year corresponds to one fifth of the capacity of a Mega-factory of 2250MW.
- Greenhouse gases not including water vapor, account for about three-quarters of the CO2 emitted by fossil fuels when they burn.
- the reduction of greenhouse gases that would be necessary to control the rise in temperatures of 2 degrees as proposed by COP21 is very difficult to achieve because there is no real way today to avoid these discharges.
- the measures to limit global warming include wind and solar which unfortunately require wind and sun to operate and produce electricity that we do not know how to store today.
- the present invention relates to a process for producing hydrogen from shale gas (or shale oil) in which:
- the produced shale gas (or oil) is converted to hydrogen by catalytic steam reforming or by partial oxygen oxidation of the air in a Mega (225 OMW) or a Giga (4.5 GW) plant located at proximity.
- the cost price of shale hydrogen thus produced and distributed is of the order of magnitude of the price of imported natural gas with equivalent energy content and this including investments with a return time of less than four years, it can therefore substitute fossil fuels today used.
- the invention thus makes it possible to reduce greenhouse gas emissions to a lower level than those expected by COP21 (United Nations Conference on Climate Change).
- the carbon mass content can vary from 65% (lignite) to 90% (coal), sulfur from 0.5 to 2%, hydrogen from 4 to 6%, water from 3 to 12%, volatile 10 to 40%, minerals from 3 (lignite) to 16%. There will therefore always ash and slag for about 10% of the load which is already the case in case of direct combustion.
- Coal gasification is based on the following main reactions:
- the actual gasification reaction is the partial oxidation of carbon by the following water: C + H 2 0 ⁇ H 2 + CO
- This reaction is what we call the carbon conversion reaction.
- the most commercialized technologies are driven fluid gasifiers with a temperature of 1400 to 1700 ° C and a pressure of 35 to 70 bar.
- the gasifier consists of a hollow chamber lined with refractory bricks.
- the single burner installed at the top of the reactor, is fed with pulverized coal, as well as steam and oxygen, the gases and the slag (10% of the supply) leave in the lower part of the apparatus.
- Oxygen is produced in an air separation unit by cryogenics.
- the gases are filtered through cyclones and / or ceramic candles which retain the particles.
- Carbonyl sulphide (COS) is then hydrolysed. Excess water is treated and sent to sulfur recovery.
- a succession of gas-to-water reactions makes it possible to adjust the CO / H2 ratio to the desired value.
- the acid gases are then extracted either by chemical, physical or combined absorption.
- the BASF solution to use an activated MDEA is very often used because of reasonable investment costs and high performance (less than 10 ppm CO2) in the synthesis gas.
- the different streams containing sulfur generally feed a unit according to Claus process which generates sulfur.
- This scheme could produce only hydrogen by adapting the gas reactions to water in a cascade of reactors, but it will be necessary to purify the hydrogen thus produced and recycle or purge the impurities (nitrogen).
- the practical hydrogen is about 1.3 moles of hydrogen for a theoretical of 2.5, which means that part of the carbon is used to heat the charge.
- the cost of a unit corresponding to an equivalent of 5000 T / d of methanol is approximately 1.5 billion euros, which is approximately 3 to 4 times the cost of a similar unit on natural gas, to which must be added the cost of sequestration of CO 2 produced.
- the amount of coal treated per hour is of the order of 250 T / h of coal at 75% by weight, ie about 2 million T / year.
- Natural gas is composed mainly of methane, so we will often talk about methane instead of natural gas in what follows.
- the main reaction is as follows:
- the natural gas is sent into the steam reformer at pressures of 20 to 30 bar, the feed is then preheated to 500-550 ° C. (examples known by the author on very small units 505 ° C. and 520 ° C).
- the steam reformer consists of tubes filled with catalyst and heated externally by burners fed with natural gas which reduces the theoretical yield.
- the synthesis gas leaves the reformer at 885 ° C, it is cooled a first time to generate 40 bar steam, it then passes through reactors (shift reactors) in which the reaction of the gas with water is carried out to convert the CO to CO2 and at the same time reduce the water to hydrogen, it is cooled a second time to preheat the water supplying the steam generator, it is finally cooled with water to 50 ° C.
- An absorption (activated M DEA-BASF method for example) is then carried out to separate the CQ 2 and reach a residual CO 2 of less than 100 ppm.
- the separated CO 2 can be compressed by a turbine driven by the steam H produced, it will then be used to carry out the fracturing in gas form or in liquid form in the hypo or hypercritical state.
- the gaseous mixture now contains residual methane, CO 2 and residual CO, hydrogen and nitrogen.
- Numerous processes make it possible to separate the hydrogen: PSA (pressure swing adsorption on molecular sieves), anaerobic digestion, membranes, cryogenic distillation, ....
- PSA pressure swing adsorption on molecular sieves
- the other compounds are recyclable in the unit subject to purging the nitrogen q ui can be used for fracturing.
- PSA can extract 85% of the hydrogen present in the mixture.
- the mixture can then be methanized to convert the residual carbon oxides to methane.
- the remaining compounds, methane, residual hydrogen and nitrogen are then separated by membrane processes, by cryogenic distillation or other processes, the methane and hydrogen will thus be fully recovered.
- the natural gas is sent to a reactor coated with refractory at pressures of 20 to 90 bar, and at temperatures of 1200 to 1500 ° C. Part of the charge is injected into a burner mounted at the top of the reactor.
- the treatment of gases leaving the reactor is similar to that of steam reforming: gas-to-water reactors, actual treatment and recycling of recoverable products.
- the reactor is a vertical cylindrical reactor on which is mounted at the top a burner and whose bottom is filled with catalyst, (ref 1)
- This reaction can be done in a prereforming.
- the reaction mechanism follows three consecutive steps:
- the ICP of the methane is 803.3 kJ / mol
- the calculation is made for a 2250MW mega plant including the corresponding part of the distribution network.
- the cost estimate is based on the following two projects.
- GTL's Oryx Qatar (ref3) manufacturing project ($ 1billion investment) includes two synthesis gas production lines equipped with autothermal reforming, which represents 2/3 of the total amount and for which air separation represents 50% . These two lines are fed by a natural gas flow of 330 million cubic feet / day corresponding to the supply of a unit of 5000T / J of methanol.
- a unit of 5000T / J of methanol has a synthesis gas manufacturing section of the same size as a unit of 5000 million Nm3 / year of hydrogen.
- the gas consumption is lower (165 MMSCFD instead of 223 MMSCFD) because the purge of the methanol reaction loop is practically enough to provide the calories necessary for reforming.
- the Atlas-Methanol Production Plant-Point Lisa-Trinidad and Tobago project (Ref 4 and Ref 5) is a MegaMethanol workshop built by Lurgi for 5000T / J of methanol at a cost of $ 400 million base 2004. This workshop reaches a capacity of 5400 t / d for a gas consumption of 175 MMSCFD in 2005. That is a cost of $ 500 million, current base, the amount is of the same order of magnitude as that extrapolated from the Oryx project.
- the price of natural gas is that of shale gas as it is given to the Henry hub, it fluctuates from $ 2 to $ 4 / MMBTU and we retain a high value of $ 3.5 / MMBTU which logically leads to a return on investment 25%, or 10.85 € / MWh PCS using an unfavorable exchange rate of 1.1 $ / €
- the variable cost includes the cost of raw materials (process gas, fuel gas, annualized load for catalysts and adsorbents) and utilities (water cooling, demineralised water, electricity, nitrogen) to which the steam credit must be deducted.
- the variable cost is 38.0 € / 1000 Nm3 of H2. Natural gas represents 90% of the cost of raw materials and utilities, which is very common for this type of unit.
- the fixed cost consists of direct fixed costs including operators, a supervisor, maintenance costs amounting to 3.5% of the investment of the conversion unit, laboratory costs as well as indirect fixed costs. amounting to 41% of direct costs. To these costs will be added the research costs, the cost of taxes and insurance, the headquarters and commercial expenses to obtain the amount of the fixed costs which is 11.1 € / 1000 Nm3 of H2.
- the cost price will be complete by including the depreciation over ten years and a return on investment of 25% per year very common in an industrial project, ie 52 € / 1000 Nm3 of H2.
- k is a characteristic coefficient of the pipe
- p is the density of the gas
- v is the velocity of the gas in the pipe.
- the ratio of pressure losses between natural gas and hydrogen is:
- Delta P hyd / Delta P gn (p hyd / p g ") * (v hyd / v gn ) 2
- An advantage of the shale hydrogen production process is that once the plants are built it can work partially with any cut from the petroleum refining process by installing a prereforming process. It can also partially be supplied with natural gas by any network.
- Reciprocally a shale gas supply of a coal gasification unit to produce synthesis gas and preferably hydrogen will separate the CO2 formed and thus sequester in the (or) shale gas drilling.
- Another advantage of this method is that it makes it possible to regulate the electricity network when the intermittent energy sources (wind and photovoltaic) produce high power by using the buffer capacities provided on the natural gas network to store the gas. shale.
- Carbon dioxide 11% forestry and other agricultural uses
- Methane 16% it comes for 67% of enteric fermentations and animal dung,
- N20 6.2% it comes from 81% of the crop with nitrogen fertilizers.
- the project consists of replacing oil and gas consumption with shale gas, since electricity production is already almost non-greenhouse gas generating and the quantities of coal used in France are specific uses ..
- a modern refinery can absorb heavy fuels. All of the listed products except heavy fuels can be converted to hydrogen and CO and thus to hydrogen by equipping the reforming of a Mega or a Giga plant with a prereformer that will convert the different cuts into a treatable mixture by the reformer.
- the main problem that requires a prereformer is the coking problem of the catalysts which is solved by installing two prereformers in parallel.
- Part of the uses are transport, electricity production, domestic uses (heating, cooking), industrial uses, those of chemistry (methanol, ammonia, ...) and polymers.
- a Mega plant produces 640500 Nm3 / h of hydrogen or 5.05 billion Nm3 / year of hydrogen, an annual power of 2250MW.
- the gas consumed corresponds to 2650 MWh PCS or 228.4 PET / h or 1.8 million PET per year.
- Ref2 Proven autothermal reforming technology for wide-scale modem methanol plant - by Per Juul Dahl-by Thomas S.Christensen- by Sandra Winter-Madsen-by Stephanie M.King Nitrogen + Syngas International Conference February 2014- Haldor Topsoe website
- Ref4 htp: // w v .chemicals-techno1og ⁇ ', com / projects / atias methanol /
- the present application thus relates to a continuous process for manufacturing hydrogen from shale gas (or shale oil) in which:
- the produced shale gas (or oil) is converted to hydrogen by catalytic steam reforming or by partial oxidation by oxygen from air in a Mega or Giga plant located nearby.
- the Mega plant has a capacity of 500 to 2250 MW, and typically 2250MW or in which the Giga plant has a capacity greater than 2250MW, and typically 4.5 GW (4500MW), the power being calculated from the PCS (higher heating value ) hydrogen.
- Hydrogen is used either directly in a power plant located on the site and (or) injected into a hydrogen pipeline, a hydrogen distribution network built for this purpose.
- the hydrogen pipeline is used to power either power plants equipped with combustion plants, gas turbines or high-power fuel cells, or distribution stations to supply motor vehicles and or semi-mounted frames - trailer.
- - shale gas (or oil) supplies a coal or lignite gasification plant producing synthesis gas and / or hydrogen and preferably hydrogen, shale gas is temporarily stored in the reservoirs planned on the natural gas network and this to allow the regulation of the electricity network when intermittent energy sources (wind and photovoltaic) produce high power.
- the conversion to hydrogen is carried out either by simple catalytic reforming, or double or by partial oxidation with oxygen in the air, or preferably by autothermal reforming (reforming coupling and partial oxidation).
- the hydrogen conversion unit is equipped with a pre-reforming process for converting any petroleum fraction into synthesis gas and / or hydrogen.
- the conversion reactor can be partially supplied with natural gas from a natural gas network.
- the CO / H2 ratio of the synthesis gas is oriented towards the production of hydrogen in one or more consecutive transformation reactors.
- the decarbonated synthesis gas undergoes complementary treatments to separate the hydrogen to reach purities of between 96 and more than 99.9% hydrogen.
- the possible treatments are very numerous: PSA (pressure swing absorption on molecular sieves, anaerobic digestion, cryogenics, separation on membranes)
- the separated compounds CH4, CO2 and residual CO
- CH4, CO2 and residual CO can be recycled or injected into the borehole (s)
- other impurities nitrogen, for example
- - IMMBTU is equivalent to 1055.06 E6 J or 0.293 MWh Icubic feet / day is equivalent to 0.028 m3 / day
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Inorganic Chemistry (AREA)
- Geology (AREA)
- Mining & Mineral Resources (AREA)
- Combustion & Propulsion (AREA)
- General Health & Medical Sciences (AREA)
- Fluid Mechanics (AREA)
- Geochemistry & Mineralogy (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Physics & Mathematics (AREA)
- Environmental & Geological Engineering (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Industrial Gases (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1600999A FR3053034A1 (fr) | 2016-06-22 | 2016-06-22 | Procede de fabrication d'hydrogene de schiste |
PCT/IB2017/053536 WO2017221113A1 (fr) | 2016-06-22 | 2017-06-14 | Procédé de fabrication d'hydrogène de schiste |
Publications (1)
Publication Number | Publication Date |
---|---|
EP3475219A1 true EP3475219A1 (fr) | 2019-05-01 |
Family
ID=58455075
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP17733904.1A Withdrawn EP3475219A1 (fr) | 2016-06-22 | 2017-06-14 | Procédé de fabrication d'hydrogène de schiste |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP3475219A1 (fr) |
FR (1) | FR3053034A1 (fr) |
WO (1) | WO2017221113A1 (fr) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3086939A1 (fr) * | 2018-10-05 | 2020-04-10 | Total Sa | Installation et procede autonome de valorisation et transformation d'hydrogene |
CN114215601B (zh) * | 2021-12-31 | 2024-01-26 | 北京派创石油技术服务有限公司 | 利用废弃油井制造氢气的方法 |
GB2616630A (en) * | 2022-03-15 | 2023-09-20 | Equinor Energy As | Hydrocarbon production system with reduced carbon dioxide emission |
CN115818569B (zh) * | 2022-11-17 | 2024-01-26 | 西南石油大学 | 一种难动用稠油/页岩油火烧制氢的方法 |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20030146002A1 (en) * | 2001-04-24 | 2003-08-07 | Vinegar Harold J. | Removable heat sources for in situ thermal processing of an oil shale formation |
EP2490792B1 (fr) * | 2009-10-24 | 2018-06-06 | Calix Limited | Système et procédé de traitement d'un gaz combustible d'entrée et de vapeur pour la production de dioxyde de carbone et d'un gaz combustible de sortie |
EP3032027B1 (fr) * | 2013-08-06 | 2019-10-09 | Chiyoda Corporation | Système d'alimentation en hydrogène et procédé d'alimentation en hydrogène |
AU2014363523B2 (en) * | 2013-12-12 | 2018-02-15 | Haldor Topsoe A/S | Process for the production of synthesis gas |
-
2016
- 2016-06-22 FR FR1600999A patent/FR3053034A1/fr not_active Withdrawn
-
2017
- 2017-06-14 EP EP17733904.1A patent/EP3475219A1/fr not_active Withdrawn
- 2017-06-14 WO PCT/IB2017/053536 patent/WO2017221113A1/fr unknown
Also Published As
Publication number | Publication date |
---|---|
FR3053034A1 (fr) | 2017-12-29 |
WO2017221113A1 (fr) | 2017-12-28 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
Muradov | Low to near-zero CO2 production of hydrogen from fossil fuels: Status and perspectives | |
US7918906B2 (en) | Compact natural gas steam reformer with linear countercurrent heat exchanger | |
CN102667057B (zh) | 整合的强化采油方法 | |
Rahimpour et al. | Feasibility of flare gas reformation to practical energy in Farashband gas refinery: No gas flaring | |
CN102597417B (zh) | 整合的强化采油方法 | |
EP3475219A1 (fr) | Procédé de fabrication d'hydrogène de schiste | |
US8236072B2 (en) | System and method for producing substitute natural gas from coal | |
CA2784876C (fr) | Procede et dispositif de production simultanee d'energie sous la forme d'electricite, de chaleur et de gaz d'hydrogene | |
CN101676368A (zh) | 化学产品提供系统及提供化学产品的方法 | |
CN107461606A (zh) | 一种在天然气输气管道中存储电能的方法 | |
US20110124748A1 (en) | Coal and Biomass Conversion to Multiple Cleaner Energy Solutions System producing Hydrogen, Synthetic Fuels, Oils and Lubricants, Substitute Natural Gas and Clean Electricity | |
CA2739274C (fr) | Reformeur a vapeur compact de gaz naturel et methode de reformage avec echangeur de chaleur lineaire a- contre-courant | |
FR2900934A1 (fr) | Procede de coproduction d'electricite et d'un gaz riche en hydrogene par vaporeformage d'une coupe hydrocarbure avec apport de calories par combustion a l'hydrogene in situ | |
Aresta et al. | The Carbon Dioxide Revolution | |
Tetteh et al. | The Blue Hydrogen Economy: A Promising Option for the Near-to-Mid-Term Energy Transition | |
Panichkittikul et al. | Improvement of biohydrogen production from biomass using supercritical water gasification and CaO adsorption | |
Alsunousi et al. | The role of hydrogen in synthetic fuel production strategies | |
EP2223888B1 (fr) | Procédé de production d'hydrogène avec captation totale du CO2, et réduction du méthane non converti | |
FR2942145A1 (fr) | Procede de recuperation de co2 d'un gaz industriel | |
CN107810252A (zh) | 用于制造甲烷的结合水的水解作用的布杜阿尔反应 | |
Qian et al. | Integration of biomass gasification and O2/H2 separation membranes for H2 production/separation with inherent CO2 capture: Techno-economic evaluation and artificial neural network based multi-objective optimization | |
Lauf | Replacing NATO F-34: Technologies and economic aspects of using secondary carbon sources for Power-to-Fuel production | |
TWI386365B (zh) | 富氫與純氫氣體製造之整合裝置與方法 | |
Dushime | Study of the adsorption performance of modified activated carbons and biochars under static and dynamic conditions for the separation of carbon dioxide (CO2) and methane (CH4) from a synthetic biogas. | |
Marcon | Applications of Ru-based catalyst for CO2 methanation: modeling study |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: UNKNOWN |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE |
|
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 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE |
|
17P | Request for examination filed |
Effective date: 20190112 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AL 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 RS SE SI SK SM TR |
|
AX | Request for extension of the european patent |
Extension state: BA ME |
|
DAV | Request for validation of the european patent (deleted) | ||
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: 20200922 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: EXAMINATION IS IN PROGRESS |
|
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: 20240103 |