FR3013819A1 - PROCESS FOR THE PRODUCTION OF CARBON MONOXIDE FROM TWO SEPARATION APPARATUS EACH PRODUCING CARBON MONOXIDE AT A DIFFERENT PURITY LEVEL - Google Patents
PROCESS FOR THE PRODUCTION OF CARBON MONOXIDE FROM TWO SEPARATION APPARATUS EACH PRODUCING CARBON MONOXIDE AT A DIFFERENT PURITY LEVEL Download PDFInfo
- Publication number
- FR3013819A1 FR3013819A1 FR1361674A FR1361674A FR3013819A1 FR 3013819 A1 FR3013819 A1 FR 3013819A1 FR 1361674 A FR1361674 A FR 1361674A FR 1361674 A FR1361674 A FR 1361674A FR 3013819 A1 FR3013819 A1 FR 3013819A1
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- Prior art keywords
- carbon monoxide
- purity
- flow
- nitrogen
- production
- 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.)
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Classifications
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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
- 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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- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/02—Mixing or blending of fluids to yield a certain product
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/50—Arrangement of multiple equipments fulfilling the same process step in parallel
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/80—Retrofitting, revamping or debottlenecking of existing plant
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Dans un procédé de production d'un débit contenant au moins 80% de monoxyde de carbone, on produit dans un premier appareil de séparation (U1) par distillation cryogénique un premier débit de monoxyde de carbone (3) ayant une première pureté en monoxyde de carbone et contenant X% d'azote, on produit dans un deuxième appareil de séparation (U2) par distillation cryogénique un deuxième débit de monoxyde de carbone (5) ayant une deuxième pureté en monoxyde de carbone, supérieure à la première pureté et contenant moins que X% d'azote et on mélange le premier et le deuxième débits pour former un débit (7) ayant une troisième pureté en monoxyde de carbone supérieure à la première pureté et inférieure à la deuxième pureté.In a process for producing a flow rate containing at least 80% carbon monoxide, a first carbon monoxide flow (3) having a first carbon monoxide purity is produced in a first separation apparatus (U1) by cryogenic distillation. carbon and containing X% of nitrogen, a second flow rate of carbon monoxide (5) having a second purity of carbon monoxide, higher than the first purity and containing less, is produced in a second separating apparatus (U2) by cryogenic distillation. X% nitrogen and mixing the first and second flow rates to form a flow (7) having a third purity carbon monoxide higher than the first purity and lower than the second purity.
Description
La présente invention est relative à un procédé de production d'un débit contenant au moins 80% de monoxyde de carbone. La présente invention est en particulier relative à un procédé de production de monoxyde de carbone a partir de deux appareils de séparation, chacun produisant du monoxyde de carbone à un niveau de pureté différente. Les pourcentages mentionnés dans ce document relatifs à des puretés sont des pourcentages molaires. Les unités de production de monoxyde de carbone et d'hydrogène peuvent être séparées en deux parties : - génération du gaz de synthèse (mélange contenant H2, CO, CH4, CO2, Ar et N2 essentiellement). Parmi les diverses voies industrielles de production de gaz de synthèse, les plus développées utilisent le gaz naturel comme matière première telles que : les fours de reformage, les réacteurs auto thermiques ou les réacteurs d'oxydation partielle. D'autres voies industrielles qui se développent de plus en plus utilisent le charbon comme matière première qui nécessite un gaz vecteur vers le réacteur. - purification du gaz de synthèse. On retrouve : - une unité de lavage à un solvant liquide pour éliminer la plus grande partie des gaz acides contenus dans le gaz de synthèse - une unité d'épuration sur lit d'adsorbants. - une unité de séparation par voie cryogénique dite boite froide pour la production de CO. La plupart des unités existantes de séparation cryogénique de mélange H2 et 25 CO n'incluent pas de séparation CO et N2 car les teneurs en N2 dans le gaz de synthèse sont compatibles avec la pureté du CO requise par l'unité en aval. Lorsque l'on souhaite sur un site existant augmenter le débit de production et la pureté du CO, il est envisageable d'investir dans deux boites froides, chacune contenant un appareil de séparation fonctionnant à basse température : un appareil 30 de séparation pour séparer l'azote du CO impur produit par l'appareil de séparation existant et un appareil de séparation qui comprend une colonne CO/N2 pour les besoins supplémentaires. Comme la teneur en N2 dans la matière première a tendance à augmenter dans le temps (la teneur de N2 augmente dans le gaz naturel, on utilise de l'azote comme 35 fluide porteur du charbon ...), la pureté du CO des unités de séparation cryogéniques existantes se dégrade et conduit a des pertes de rendements de production des produits qui consomment le CO. Bien souvent sur un site de production existant, on est confronté à l'augmentation de production de CO pour suivre le développement des produits qui en sont consommateurs et à l'augmentation de la teneur de l'azote dans le gaz de charge. Afin d'augmenter la production et la productivité des unités avals qui consomment du CO, on est amené sur un même site industriel à augmenter à la fois le débit de production de CO et sa pureté.The present invention relates to a method for producing a flow rate containing at least 80% carbon monoxide. In particular, the present invention relates to a process for producing carbon monoxide from two separation devices, each producing carbon monoxide at a different purity level. The percentages mentioned in this document relating to purities are molar percentages. The production units for carbon monoxide and hydrogen can be separated into two parts: - generation of the synthesis gas (mixture containing H2, CO, CH4, CO2, Ar and N2 essentially). Among the various synthetic gas production lines, the most developed use natural gas as raw material such as: reforming furnaces, auto-thermal reactors or partial oxidation reactors. Other industrial processes that are developing more and more use coal as raw material that requires a carrier gas to the reactor. - purification of the synthesis gas. We find: - a washing unit with a liquid solvent to remove most of the acid gases contained in the synthesis gas - an adsorbent bed purification unit. - A cryogenic separation unit called cold box for the production of CO. Most existing units for cryogenic separation of H2 and CO mixtures do not include CO and N2 separation because the N2 contents in the synthesis gas are compatible with the CO purity required by the downstream unit. When it is desired on an existing site to increase the production rate and the purity of the CO, it is conceivable to invest in two cold boxes, each containing a separation apparatus operating at low temperature: a separating apparatus for separating the impure CO nitrogen produced by the existing separation apparatus and separation apparatus which includes a CO / N2 column for additional requirements. Since the N 2 content in the raw material tends to increase over time (the content of N 2 increases in natural gas, nitrogen is used as the carrier fluid for coal ...), the purity of the CO of the units existing cryogenic separation is degraded and leads to losses in production yields of products that consume CO. Often on an existing production site, one is confronted with the increase of CO production to follow the development of the products which are consumers of it and with the increase of the nitrogen content in the charge gas. In order to increase the production and the productivity of the downstream units which consume CO, one is brought on the same industrial site to increase at the same time the rate of production of CO and its purity.
L'idée de la présente invention est d'investir dans un appareil de séparation qui comprend une séparation permettant d'épurer le monoxyde de carbone en azote mais dont la capacité est supérieure aux nouveaux besoins. L'invention consiste à opérer l'appareil de séparation existant à charge réduite et de mélanger les deux débits de monoxyde de carbone produits par l'appareil de séparation existant et le nouvel appareil de séparation. Ceci permet de réduire l'investissement par rapport à l'état de l'art. Selon un objet de l'invention, il est prévu un procédé de production d'un débit contenant au moins 80% de monoxyde de carbone dans lequel : i) on produit dans un premier appareil de séparation par distillation cryogénique un premier débit de monoxyde de carbone ayant une première pureté en monoxyde de carbone et contenant X% d'azote ii) on produit dans un deuxième appareil de séparation par distillation cryogénique un deuxième débit de monoxyde de carbone ayant une deuxième pureté en monoxyde de carbone, supérieure à la première pureté et contenant 25 moins que X% d'azote et iii) on mélange le premier et le deuxième débits pour former un débit ayant une troisième pureté en monoxyde de carbone supérieure à la première pureté et inférieure à la deuxième pureté.Selon d'autres aspects facultatifs : - le premier appareil est capable de produire le premier débit avec un débit 30 maximal D à la première pureté et l'on fait fonctionner le premier appareil pour produire un débit inférieur à D et ayant la première pureté. - l'on fait fonctionner le premier appareil pour produire le premier débit avec un débit inférieur à 3D/4. - le deuxième appareil fonctionne à sa capacité maximale. - le deuxième appareil produit le deuxième débit au moyen d'une colonne de distillation d'où sont soutirés le monoxyde de carbone à la deuxième pureté et un débit contenant au moins 50% d'azote. - le premier appareil produit le premier débit au moyen d'une colonne de distillation d'où sont soutirés le monoxyde de carbone à la première pureté et un débit contenant au moins 50% d'hydrogène ou de méthane ou d'azote. - la première pureté est inférieure à 96% de monoxyde de carbone et/ou la deuxième pureté est supérieure à 98% de monoxyde de carbone. - le premier appareil est disposé à l'intérieur d'une première enceinte isolée - le deuxième appareil est disposé à l'intérieur d'une deuxième enceinte isolée L'invention sera décrite de manière plus détaillée par rapport à la figure qui montre un procédé selon l'invention.The idea of the present invention is to invest in a separation apparatus which comprises a separation for purifying carbon monoxide to nitrogen but whose capacity is greater than the new requirements. The invention involves operating the existing reduced-load separation apparatus and mixing the two carbon monoxide flow rates produced by the existing separation apparatus and the new separation apparatus. This reduces the investment compared to the state of the art. According to one object of the invention, there is provided a method for producing a flow rate containing at least 80% carbon monoxide in which: i) a first flow of carbon monoxide is produced in a first separation apparatus by cryogenic distillation carbon having a first carbon monoxide purity and containing X% nitrogen ii) producing in a second cryogenic distillation separation apparatus a second flow of carbon monoxide having a second purity of carbon monoxide, higher than the first purity and containing less than X% of nitrogen and iii) mixing the first and second flow rates to form a flow rate having a third carbon monoxide purity higher than the first purity and lower than the second purity.According to other aspects optional: the first apparatus is capable of producing the first flow with a maximum flow D at the first purity and the first apparatus is operated to produce a flow rate lower than D and having the first purity. the first apparatus is operated to produce the first flow rate with a flow rate less than 3D / 4. - the second device operates at its maximum capacity. the second apparatus produces the second flow by means of a distillation column from which carbon monoxide at the second purity is withdrawn and a flow rate containing at least 50% of nitrogen. the first apparatus produces the first flow by means of a distillation column from which carbon monoxide at the first purity is withdrawn and a flow rate containing at least 50% of hydrogen or methane or nitrogen. the first purity is less than 96% carbon monoxide and / or the second purity is greater than 98% carbon monoxide. the first apparatus is disposed inside a first insulated enclosure; the second device is placed inside a second insulated enclosure. The invention will be described in more detail with respect to the figure which shows a process. according to the invention.
Un appareil de distillation cryogénique U1 existant était capable de produire du monoxyde de carbone 3 avec une pureté de 98.5% mais la pureté du gaz de synthèse qui l'alimente a dégradé et contient plus d'azote qu'avant. Ainsi l'appareil U1 a une capacité maximale de 9800 Nm3/h mais avec une pureté de seulement 94,15% pour le gaz 3 L'appareil de distillation peut être un appareil de condensation partielle, de lavage au méthane ou de lavage au monoxyde de carbone. La colonne d'où est soutiré le gaz 3 produit également un débit contenant au moins 50% d'hydrogène ou de méthane ou d'azote. Maintenant le client a besoin de 14250 Nm3/h de monoxyde de carbone à la pureté de 98.5%. Selon l'invention, on rajoute un deuxième appareil de distillation cryogénique U2 alimenté par le gaz de synthèse et comprenant une colonne qui produit le gaz 5 avec une pureté de 99.9% et un débit de 8500Nm3/h. La colonne produit également un débit contenant au moins 50% d'azote.An existing U1 cryogenic distillation apparatus was capable of producing carbon monoxide 3 with a purity of 98.5% but the purity of the synthesis gas which feeds it has degraded and contains more nitrogen than before. Thus the apparatus U1 has a maximum capacity of 9800 Nm3 / h but with a purity of only 94.15% for the gas 3 The distillation apparatus may be a partial condensation device, methane washing or monoxide washing of carbon. The column from which the gas 3 is withdrawn also produces a flow rate containing at least 50% hydrogen or methane or nitrogen. Now the customer needs 14250 Nm3 / h of carbon monoxide at purity of 98.5%. According to the invention, there is added a second cryogenic distillation apparatus U2 fed by the synthesis gas and comprising a column which produces the gas with a purity of 99.9% and a flow rate of 8500 Nm3 / h. The column also produces a flow rate containing at least 50% nitrogen.
L'appareil U2 opère à sa capacité maximale. Par contre l'appareil U1 ne produit que 5750 Nm3/h de gaz 3 à 94,15% car il fonctionne à 59% de sa capacité maximale. Les débits 3,5 sont mélangés pour produire 14250 Nm3/h de monoxyde de carbone à la pureté de 98.5%, comme requis par le client.35The U2 device operates at its maximum capacity. On the other hand, the U1 apparatus produces only 5750 Nm3 / h of gas 3 at 94.15% because it operates at 59% of its maximum capacity. The 3.5 flow rates are mixed to produce 14250 Nm3 / h of carbon monoxide at 98.5% purity, as required by the customer.
Claims (10)
Priority Applications (1)
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FR1361674A FR3013819A1 (en) | 2013-11-27 | 2013-11-27 | PROCESS FOR THE PRODUCTION OF CARBON MONOXIDE FROM TWO SEPARATION APPARATUS EACH PRODUCING CARBON MONOXIDE AT A DIFFERENT PURITY LEVEL |
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FR1361674A FR3013819A1 (en) | 2013-11-27 | 2013-11-27 | PROCESS FOR THE PRODUCTION OF CARBON MONOXIDE FROM TWO SEPARATION APPARATUS EACH PRODUCING CARBON MONOXIDE AT A DIFFERENT PURITY LEVEL |
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FR3013819A1 true FR3013819A1 (en) | 2015-05-29 |
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FR1361674A Pending FR3013819A1 (en) | 2013-11-27 | 2013-11-27 | PROCESS FOR THE PRODUCTION OF CARBON MONOXIDE FROM TWO SEPARATION APPARATUS EACH PRODUCING CARBON MONOXIDE AT A DIFFERENT PURITY LEVEL |
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Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3814293A1 (en) * | 1988-04-28 | 1989-11-09 | Linde Ag | Process for recovering carbon monoxide |
US5017204A (en) * | 1990-01-25 | 1991-05-21 | Air Products And Chemicals, Inc. | Dephlegmator process for the recovery of helium |
US6098424A (en) * | 1998-02-20 | 2000-08-08 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and plant for production of carbon monoxide and hydrogen |
US20060190113A1 (en) * | 2004-12-10 | 2006-08-24 | Florence Boutemy | Novel network production planning method |
DE102010049444A1 (en) * | 2010-10-23 | 2012-04-26 | Linde Aktiengesellschaft | Method for cooling cryogenic part of cryogenic gas decomposer for e.g. methane laundry, involves removing carbon monoxide from external carbon monoxide source, and introducing carbon monoxide as circulatory medium into cooling circuit |
-
2013
- 2013-11-27 FR FR1361674A patent/FR3013819A1/en active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3814293A1 (en) * | 1988-04-28 | 1989-11-09 | Linde Ag | Process for recovering carbon monoxide |
US5017204A (en) * | 1990-01-25 | 1991-05-21 | Air Products And Chemicals, Inc. | Dephlegmator process for the recovery of helium |
US6098424A (en) * | 1998-02-20 | 2000-08-08 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and plant for production of carbon monoxide and hydrogen |
US20060190113A1 (en) * | 2004-12-10 | 2006-08-24 | Florence Boutemy | Novel network production planning method |
DE102010049444A1 (en) * | 2010-10-23 | 2012-04-26 | Linde Aktiengesellschaft | Method for cooling cryogenic part of cryogenic gas decomposer for e.g. methane laundry, involves removing carbon monoxide from external carbon monoxide source, and introducing carbon monoxide as circulatory medium into cooling circuit |
Non-Patent Citations (1)
Title |
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BERNINGER R: "FORTSCHRITTE BEI DER H2/CO-TIEFTEMPERATURZERLEGUNG//PROGRESS IN H2/CO LOW TEMPERATURE SEPARATION", BERICHTE AUS TECHNIK UND WISSENSCHAFT, LINDE AG. WIESBADEN, DE, vol. 62, 1 January 1988 (1988-01-01), pages 18 - 32, XP009045782, ISSN: 0942-332X * |
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