FR3071827A3 - PROCESS FOR THE PRODUCTION OF A RICH CARBON MONOXIDE PRODUCT - Google Patents
PROCESS FOR THE PRODUCTION OF A RICH CARBON MONOXIDE PRODUCT Download PDFInfo
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- FR3071827A3 FR3071827A3 FR1857981A FR1857981A FR3071827A3 FR 3071827 A3 FR3071827 A3 FR 3071827A3 FR 1857981 A FR1857981 A FR 1857981A FR 1857981 A FR1857981 A FR 1857981A FR 3071827 A3 FR3071827 A3 FR 3071827A3
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/40—Carbon monoxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0261—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon monoxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/32—Compression of the product stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/02—Internal refrigeration with liquid vaporising loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
Abstract
Une colonne de séparation d'azote et de monoxyde de carbone à température cryogénique comprend un condenseur de tête (C2) et un condenseur intermédiaire (C1), les deux étant refroidis par le liquide de cuve 29 de la colonne.A nitrogen and carbon monoxide separation column at cryogenic temperature comprises a top condenser (C2) and an intermediate condenser (C1), both of which are cooled by the bottom liquid 29 of the column.
Description
La présente invention est relative à un procédé et à une installation pour la production d’un produit riche en monoxyde de carbone à deux pressions à partir d’un mélange de monoxyde de carbone, d’azote et d’hydrogène.The present invention relates to a process and an installation for the production of a product rich in carbon monoxide at two pressures from a mixture of carbon monoxide, nitrogen and hydrogen.
Le mélange est séparé à température cryogénique par séparation des phases et ensuite par distillation.The mixture is separated at cryogenic temperature by phase separation and then by distillation.
Il est connu d’utiliser des procédés de type condensation partielle pour séparer un gaz de synthèse comprenant du monoxyde de carbone et de l’hydrogène afin de récupérer un produit riche en hydrogène et un produit riche en CO. Suivant la pureté requise sur le produit CO, il est possible de rajouter des colonnes afin de purifier le CO au niveau requis (par exemple ne colonne de séparation de CO/CH4 ou une colonne de séparation de CO/N2)It is known to use partial condensation processes to separate a synthesis gas comprising carbon monoxide and hydrogen to recover a hydrogen-rich product and a product rich in CO. Depending on the required purity of the CO product, it is possible to add columns to purify the CO to the required level (eg CO / CH4 separation column or CO / N2 separation column)
Le principal avantage de ce procédé par rapport à un procédé de type lavage au méthane est de réduire drastiquement l’investissement.The main advantage of this process over a methane scrubbing process is to drastically reduce the investment.
Lorsque le procédé de génération du gaz de synthèse change, à cause, par exemple d’un problème de disponibilité ou du coût d’une ressource par rapport à l’autre qui a évolué avec le temps, la composition résultante du gaz de synthèse changera drastiquement. Il est donc nécessaire de réajuster le procédé de séparation du gaz de synthèse en CO et H2 à cette nouvelle composition. Néanmoins, certains éléments d’un procédé existant peuvent être réutilisés tels que le compresseur par exemple. L’objet de l’invention est de rajouter un deuxième condenseur à la colonne de séparation de CO/N2 afin de générer du CO à deux pressions. Au lieu de condenser tout le gaz montant en tête de colonne (donc à la température la plus froide), on procédera en plusieurs étapes, à différentes températures. Ainsi une partie du gaz sera condensé à un niveau intermédiaire de la colonne CO/N2 dans un condenseur. L’énergie de condensation sera donc répartie entre deux températures. Par conséquent le CO qui se sera vaporisé pour condenser le gaz de colonne pourra être produit à deux pressions différentes.When the synthesis gas generation process changes, because of, for example, a problem of availability or the cost of one resource over the other which has evolved over time, the resulting composition of the synthesis gas will change. drastically. It is therefore necessary to readjust the process for separating the synthesis gas into CO and H2 into this new composition. Nevertheless, some elements of an existing process can be reused such as the compressor for example. The object of the invention is to add a second condenser to the CO / N2 separation column in order to generate CO at two pressures. Instead of condensing all the gas rising at the top of the column (so at the coldest temperature), we will proceed in several stages, at different temperatures. Thus part of the gas will be condensed at an intermediate level of the CO / N2 column in a condenser. The condensation energy will be distributed between two temperatures. Consequently, the CO that vaporizes to condense the column gas can be produced at two different pressures.
Ainsi au lieu de produire tout le CO basse pression, on pourra en récupérer une partie à moyenne pression. On récupérera ainsi de l’énergie de compression.So instead of producing all the CO low pressure, we can recover some of the medium pressure. This will recover compression energy.
Typiquement, le gradient de température sur les colonnes CO/N2 est assez faible étant donné que les molécules CO et N2 sont physiquement très proches. Ici, étant donné que le procédé amont de la colonne CO/N2 ne consiste qu’en des condensations partielles (cf figure), il reste de l’hydrogène dans cette colonne ce qui contribuera fortement à établir un gradient thermique et donc à pouvoir condenser le gaz à deux températures différentes.Typically, the temperature gradient on the CO / N2 columns is quite low since the CO and N2 molecules are physically very close. Here, since the upstream process of the CO / N2 column consists only of partial condensations (see figure), there remains hydrogen in this column which will contribute strongly to establish a thermal gradient and thus to be able to condense the gas at two different temperatures.
Il est également possible de « polluer » le gaz montant (avec une introduction de Flash gas en milieu de colonne ou même de gaz riche en hydrogène) afin d’introduire artificiellement ce gradient thermique.It is also possible to "pollute" the rising gas (with an introduction of flash gas in the middle of the column or even of gas rich in hydrogen) in order to artificially introduce this thermal gradient.
Selon un objet de l’invention, il est prévu un procédé de séparation d’un mélange gazeux de monoxyde de carbone, d’azote et d’hydrogène dans lequel : i) Le mélange gazeux refroidi et épuré est envoyé à une colonne de séparation ii) La colonne comprend un rebouilleur de cuve, un condenseur de tête et un condenseur intermédiaire iii) Un débit riche en azote est soutiré en tête de la colonne iv) Un débit liquide riche en monoxyde de carbone est soutiré en cuve de la colonne v) Le débit liquide riche en monoxyde de carbone refroidit le condenseur intermédiaire et s’en trouve réchauffé vi) Le débit liquide réchauffé est divisé en deux vii) Une première fraction du débit liquide réchauffé est vaporisée dans un échangeur de chaleur et ensuite comprimée dans un premier compresseur viii) Une deuxième fraction du débit liquide réchauffé est détendue dans une vanne, utilisée pour refroidir le condenser de tête, réchauffée dans l’échangeur de chaleur et ensuite comprimée d’abord dans un deuxième compresseur et ensuite dans le premier condenseur. L’invention permet la production de CO, de H2, et production possible de méthane si le gaz d’alimentation en contient.According to one object of the invention, there is provided a method for separating a gaseous mixture of carbon monoxide, nitrogen and hydrogen in which: i) The cooled and purified gaseous mixture is sent to a separation column ii) The column comprises a bottom reboiler, a head condenser and an intermediate condenser iii) A nitrogen-rich flow is withdrawn at the top of the column iv) A carbon monoxide-rich liquid flow is withdrawn in the bottom of the column v ) The carbon monoxide rich liquid flow cools the intermediate condenser and is warmed vi) The heated liquid flow is divided into two vii) A first fraction of the heated liquid flow is vaporized in a heat exchanger and then compressed in a first compressor viii) A second fraction of the heated liquid flow is expanded in a valve, used to cool the condenser overhead, heated in the heat exchanger heat and then compressed first into a second compressor and then into the first condenser. The invention allows the production of CO, H2, and possible production of methane if the feed gas contains it.
En utilisant deux condensations sur la colonne CO/N2, ceci permet : o La production de CO à deux pressions afin d’économiser de l’énergie de recompression o La possibilité de moduler entre les quantités de CO produites à chaque pression afin de réutiliser un compresseur existant. L’installation du condenseur intermédiaire est faite au moyen : o D’une garde hydraulique dans la colonne pour forcer le gaz à passer par ce condenseur intermédiaire, o D’un déphlégmateur installé dans la colonne ou en dehors (en hauteur par rapport au point de piquage.). L’invention sera décrite en plus de détail en se référant aux figures.By using two condensations on the CO / N2 column, this allows: o The production of CO at two pressures in order to save energy of recompression o The possibility of modulating between the quantities of CO produced at each pressure in order to reuse a existing compressor. The installation of the intermediate condenser is done by means of: o A hydraulic guard in the column to force the gas to pass through the intermediate condenser, o A dephlégmateur installed in the column or outside (in height relative to the point stitching). The invention will be described in more detail with reference to the figures.
La Figure 1 représente la partie froide d’un procédé de séparation d’un mélange gazeux de monoxyde de carbone, d’azote et d’hydrogène.Figure 1 shows the cold part of a process for separating a gaseous mixture of carbon monoxide, nitrogen and hydrogen.
Le mélange 1 est épuré pour enlever le dioxyde de carbone et l’eau par des adsorbants FEP régénérés par le gaz 3. Après refroidissement le gaz à séparer 5 est refroidi dans les deux échangeurs de chaleur E1, E2 et séparé dans un séparateur de phase S1. Le gaz formé 9 est refroidi dans un échangeur E3 et séparé dans un séparateur de phases S2. Le gaz formé 13 est réchauffé dans l’échangeur E3, détendu dans une turbine 7, chauffé de nouveau dans l’échangeur E3, E2 et E1 et produit comme débit riche en hydrogène. Les liquides 11,15 des séparateurs S1, S2 sont mélangés, détendu comme gaz 17 et séparés dans un séparateur de phases S3 pour produire le gaz 19. Le liquide formé 21 est divisé en deux. Une partie 27 est détendu et envoyé directement à un point intermédiaire de la colonne K1 et le reste 23 est réchauffé, chauffe la cuve de la colonne K1 via l’échangeur E4 et est envoyé également au point intermédiaire de la colonne K1.The mixture 1 is purified to remove carbon dioxide and water by FEP adsorbents regenerated by the gas 3. After cooling the gas to be separated 5 is cooled in the two heat exchangers E1, E2 and separated in a phase separator S1. The formed gas 9 is cooled in an exchanger E3 and separated in a phase separator S2. The formed gas 13 is heated in the exchanger E3, expanded in a turbine 7, heated again in the exchanger E3, E2 and E1 and produced as a flow rich in hydrogen. The liquids 11, 15 of the separators S1, S2 are mixed, expanded as gas 17 and separated in a phase separator S3 to produce the gas 19. The formed liquid 21 is divided in two. A portion 27 is expanded and sent directly to an intermediate point of the column K1 and the rest 23 is heated, heated the tank of the column K1 via the exchanger E4 and is also sent to the intermediate point of the column K1.
La colonne K1 a un condenseur de tête C2 et un condenseur intermédiaire C1. De l’azote gazeux 47 sort de la tête de la colonne et du liquide 29 riche en monoxyde de carbone de la cuve. Le liquide sert d’abord à refroidir le condenseur C1 en condensant un gaz intermédiaire de la colonne pris au-dessus de l’arrivée de l’alimentation.Column K1 has a head condenser C2 and an intermediate condenser C1. Nitrogen gas 47 exits from the top of the column and the carbon monoxide rich liquid 29 from the vessel. The liquid first serves to cool the condenser C1 by condensing an intermediate gas from the column taken above the arrival of the supply.
Le liquide 29 détendu et réchauffé est divisé en deux. Une partie 33 se réchauffe dans les échangeurs E2, E1 avant d’être envoyée au compresseur V1 pour être comprimée.The relaxed and heated liquid 29 is divided in two. A part 33 heats up in the exchangers E2, E1 before being sent to the compressor V1 to be compressed.
Une autre partie 31 est détendue dans une vanne, vaporisé dans le condenseur C2 pour former le gaz 35.Another portion 31 is expanded in a valve, vaporized in the condenser C2 to form the gas 35.
Un liquide de cuve 37 du condenseur est détendu et envoyé à un séparateur de phases S4. Le gaz formé 41 est mélangé avec le gaz 35 Le liquide 39 est réchauffé au bout froid de l’échangeur E2.A tank liquid 37 of the condenser is expanded and sent to a phase separator S4. The formed gas 41 is mixed with the gas. The liquid 39 is heated at the cold end of the exchanger E2.
Le gaz 43 formant en mélangeant les gaz 41 et 35 est réchauffé dans l’échangeur E1 et envoyé à un compresseur V2 dont le gaz comprimé alimente également le compresseur V1 pour produire le produit 45 riche en monoxyde de carbone.The gas 43 forming by mixing the gases 41 and 35 is heated in the exchanger E1 and sent to a compressor V2 whose compressed gas also feeds the compressor V1 to produce the product 45 rich in carbon monoxide.
La Figure 2 illustre le schéma global avec épuration du mélange 1 dans l’épuration FEP et séparation dans la boîte froide CB contenant les échangeurs, séparateurs de phase et la colonne.FIG. 2 illustrates the overall scheme with purification of the mixture 1 in the FEP purification and separation in the cold box CB containing the exchangers, phase separators and the column.
Claims (2)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR1857981A FR3071827B3 (en) | 2018-09-06 | 2018-09-06 | PROCESS FOR THE PRODUCTION OF A PRODUCT RICH IN CARBON MONOXIDE |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR1857981A FR3071827B3 (en) | 2018-09-06 | 2018-09-06 | PROCESS FOR THE PRODUCTION OF A PRODUCT RICH IN CARBON MONOXIDE |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| FR3071827A3 true FR3071827A3 (en) | 2019-04-05 |
| FR3071827B3 FR3071827B3 (en) | 2020-04-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| FR1857981A Active FR3071827B3 (en) | 2018-09-06 | 2018-09-06 | PROCESS FOR THE PRODUCTION OF A PRODUCT RICH IN CARBON MONOXIDE |
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| Country | Link |
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| FR (1) | FR3071827B3 (en) |
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- 2018-09-06 FR FR1857981A patent/FR3071827B3/en active Active
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| Publication number | Publication date |
|---|---|
| FR3071827B3 (en) | 2020-04-17 |
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