EP3368846A1 - Method and apparatus for separating a synthesis gas - Google Patents

Method and apparatus for separating a synthesis gas

Info

Publication number
EP3368846A1
EP3368846A1 EP16809945.5A EP16809945A EP3368846A1 EP 3368846 A1 EP3368846 A1 EP 3368846A1 EP 16809945 A EP16809945 A EP 16809945A EP 3368846 A1 EP3368846 A1 EP 3368846A1
Authority
EP
European Patent Office
Prior art keywords
gas
synthesis gas
carbon monoxide
enriched
compressor
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Withdrawn
Application number
EP16809945.5A
Other languages
German (de)
French (fr)
Inventor
Bertrand DEMOLLIENS
Antoine Hernandez
Jean-Marc Tsevery
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP3368846A1 publication Critical patent/EP3368846A1/en
Withdrawn legal-status Critical Current

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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
    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • 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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    • 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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    • 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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    • F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
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    • 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
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
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    • C01B2203/046—Purification by cryogenic separation
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
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    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
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    • 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
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
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    • 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
    • C01B2203/0495—Composition of the impurity the impurity being water
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0001—Separation or purification processing
    • C01B2210/0009—Physical processing
    • C—CHEMISTRY; METALLURGY
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    • C01B2210/0051—Carbon dioxide
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    • 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
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/18—H2/CO mixtures, i.e. synthesis gas; Water gas, shifted synthesis gas or purge gas from HYCO synthesis
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Definitions

  • the present invention relates to a method and apparatus for separating a synthesis gas.
  • the synthesis gas comprises carbon monoxide and hydrogen and optionally methane and / or nitrogen
  • a cryogenic distillation apparatus is supplied with synthesis gas by a synthesis gas generation unit such as reforming or / and partial oxidation (SMR, ATR, POX, ).
  • the synthesis gas at the output of the generation unit is cooled (for the production of steam and various preheaters and possibly by cooling water) and then sent to a CO 2 extraction system (typically by washing with amines such as MEA, MDEA, aMDEA) and then dried before being sent to the cryogenic distillation apparatus for CO separation and purification.
  • the residual gas called AOG or "acetylene offgas" in English is the synthesis gas. It is compressed with a compressor upstream of the cryogenic distillation apparatus. The pressure at which this gas is compressed is compatible with the hydrogen-rich product pressure required. Thus, it is not mandatory to recompress the hydrogen before it is transferred to the customer.
  • the synthesis gas generation part delivers only the requested CO molecules (in order not to degrade the operating costs and to avoid as much as possible to put in the torch of surplus CO and / or H2 products).
  • the cryogenic distillation apparatus will operate at a low rate, expressed as a ratio of the flow rate of CO and / or H2 to the nominal flow rates.
  • the operating stability of the cryogenic distillation apparatus at low load over the long term poses a problem with increased risks of not respecting the required purity of the CO or having too fluctuating production rates.
  • it is necessary to operate it with a sufficient charge rate which may be greater than the specific needs of the customers.
  • the costs are degraded by having to operate the cryogenic distillation apparatus at a level of load higher than the needs of the customers.
  • cryogenic distillation apparatus In the production of carbon monoxide and hydrogen from a synthesis gas generated by reforming or partial oxidation, a cryogenic distillation apparatus and an adsorption unit are generally used.
  • the cryogenic distillation apparatus purifies the CO and produces a hydrogen enriched flow which is then purified to hydrogen by adsorption.
  • the proposed solution is to recycle gases produced by the cryogenic distillation apparatus, possibly all the gases produced by the cryogenic distillation apparatus, upstream of the cryogenic distillation apparatus.
  • the separation units are not stopped and when the synthesis gas generating source returns to operation, it becomes possible to reprocess the synthesis gas and produce the required products.
  • This solution also makes it possible to ensure descending loads of up to 0% of the source without stopping instead of typically 40%.
  • a process for separating a synthesis gas containing carbon monoxide and hydrogen in which: i) compressing a flow of synthesis gas from a source of synthesis gas into a compressor
  • the cooled synthesis gas flow is separated by washing and / or distillation at a cryogenic temperature and optionally by adsorption in a separation unit and
  • At least the following three gases are produced in the separation unit: a carbon monoxide enriched gas, a hydrogen enriched gas, a carbon monoxide containing waste gas and a less pure carbon monoxide gas that the gas enriched in carbon monoxide and less pure hydrogen than the gas enriched in hydrogen and optionally also a gas enriched in methane, and / or a nitrogen-enriched gas characterized in that only if the flow of synthesis gas sent at the compressor is below a threshold or zero, at least a portion of at least two or even of each of the following three gases is sent: the carbon monoxide enriched gas, the hydrogen enriched gas and the monoxide-containing waste gas carbon and hydrogen downstream of the source, and possibly upstream of the compressor, to be purified in the purification unit and separated in the separation unit.
  • step v) at least a portion of the compressed synthesis gas and at least a part of at least each of the first three gases of step v) downstream of the source, and possibly upstream of the compressor, are sent to be purified in the purification unit and separated in the separation unit.
  • the outputs of the separation unit are nominal productions
  • carbon monoxide enriched gas is sent to a customer if the synthesis gas flow rate is above the threshold and carbon monoxide enriched gas from the storage is sent to the customer if the synthesis gas flow rate is lower than the threshold. threshold.
  • the synthesis gas is a waste gas from an acetylene production unit. if the flow rate of synthesis gas is greater than the threshold, a part of the synthesis gas is stored in a storage and if the flow rate of synthesis gas is below the threshold, synthesis gas is sent from the storage to the compressor.
  • the separation unit is fed solely by gases produced by the separation unit.
  • the carbon monoxide enriched gas is compressed in a product compressor and sent to the customer and if the synthesis gas flow rate is below the threshold and the carbon monoxide enriched gas flow rate to be compressed is less than another At the threshold, nitrogen gas is sent to the product compressor to be compressed with the carbon monoxide enriched gas.
  • a rich gas is sent to a synthesis gas component from another source that is not the separation apparatus to the separation unit.
  • the carbon monoxide enriched gas is compressed in a compressor, then divided into two, a compressed portion serving as a product and a compressed portion being recycled downstream of the source and / or the hydrogen-enriched gas is compressed in a compressor, then divided in two, a compressed portion serving as a product and a compressed portion being recycled downstream of the source.
  • an apparatus for separating a synthesis gas containing carbon monoxide and hydrogen comprising a compressor for compressing a flow of synthesis gas from a gas source. of synthesis, a purification unit for purifying the compressed synthesis gas, water, and / or carbon dioxide, means for cooling the compressed and purified synthesis gas flow, a separation unit of the synthesis gas flow cooled by washing and / or distillation at a cryogenic temperature optionally comprising an adsorption unit, means for producing separation unit at least the following three gases: a gas enriched in carbon monoxide, a gas enriched in hydrogen, a gas carbon monoxide and hydrogen less pure carbon monoxide than the carbon monoxide enriched and less pure hydrogen gas than the hydrogen enriched gas and optionally also a gas enriched in methane, and / or a gas enriched in nitrogen, means for sending at least a portion of at least two or even of each of the three gases carbon monoxide enriched gas, the hydrogen-enriched gas and the carbon mon
  • the apparatus comprises:
  • this storage being connected to the inlet duct of the compressor by means not passing through the compressor.
  • the synthesis gas compressor is used to recycle the fluids produced by the cryogenic distillation apparatus in order to:
  • a buffer capacity of CO gas may be added. Indeed, the gases produced by the apparatus of Cryogenic distillation will then be recycled and the gas required by the customer will then come from this buffer capacity installed upstream of the control valve on the CO production line and will be operated at a pressure greater than the pressure required by the unit that consumes the CO.
  • Nitrogen may be injected at the CO compressor suction to counterbalance compressor leakage. We will prefer
  • a synthesis gas 1 comes from a synthesis gas generation unit, for example, a reforming unit, such as an SMR or an ATR or a partial oxidation unit, which produces, for example acetylene.
  • the synthesis gas 1 contains carbon monoxide, carbon dioxide, hydrogen and optionally methane and nitrogen.
  • the gas 1 is compressed by a compressor 3 to form a compressed gas 5.
  • the compressed gas 5 is sent to a treatment unit 7 by hydrogenation to remove oxygen and unsaturated hydrocarbons producing a flow rate 9.
  • the flow 9 is sent to a CO2 purification unit 13, for example by washing with amines producing a purge flow rich in CO2 1 1 and a depleted synthesis gas flow rate
  • the flow rate 15 is fed to an adsorption CO 2 purification unit 17 to remove the remaining CO 2.
  • the CO2 purified synthesis gas 19 is sent to a cryogenic distillation unit 21 where the synthesis gas is cooled and then separated in at least one distillation column, comprising for example a methane washing step and / or partial condensation and / or carbon monoxide wash.
  • the cryogenic distillation unit 21 produces a gas flow enriched in carbon monoxide 26, a gas rich in hydrogen 27 and a waste gas 23 containing carbon monoxide and hydrogen, less pure carbon monoxide than the gas 26 and less pure hydrogen than gas 27.
  • the carbon monoxide enriched gas stream 26 is compressed in a compressor 33.
  • a gas flow 31 from the outlet of the compressor 33 is returned to the cryogenic distillation unit 21.
  • 37 shows losses of the carbon monoxide enriched gas from the compressor 33.
  • the gas from an intermediate stage of the compressor 33 partially forms a product.
  • the outputs of the separation unit are nominal productions
  • a percentage of x% of the carbon monoxide-rich gas, y% of the hydrogen-rich gas and z% of the waste gas may be returned to the purification unit and then to the cryogenic separation.
  • the percentages x, y and z are preferably the same but may differ by less than 5%.
  • nitrogen gas can be injected at an intermediate level or at the suction of the compressor 33 to compensate for compressor leakage.
  • Figure 2 differs from Figure 1 in that the hydrogen enriched flow is fed from the adsorption unit 17 which removes water and CO 2 to an adsorption purification apparatus 41.
  • This apparatus 41 produces a gas.
  • the hydrogen-depleted gas 47 from the apparatus 41 is mixed with the waste 49 of the apparatus 21 and compressed in a compressor 53 to provide a pressurized waste gas.
  • the synthesis gas 1 is no longer produced or is produced in a reduced amount, at least some products of the cryogenic distillation apparatus 21 are recycled upstream of the compressor 3, possibly after an additional treatment step.
  • at least a portion 45 of the hydrogen-rich product 43 and / or at least a portion of the hydrogen-rich product 43 can be recycled upstream of the compressor 3 waste gas from the compressor 53.
  • FIG. 3 differs from FIG. 1 in that part 4 of synthesis gas is taken at an intermediate pressure of compressor 3 for part 4 and at the final pressure thereof for part 4 and is not treated. in units 7,13,17,21.
  • Part 4 is sent from the final pressure of the compressor 3 to an adsorption separation unit called PSA 16 where it is purified to form a hydrogen-rich flow 52.
  • PSA 16 adsorption separation unit
  • the waste 18 of the hydrogen-depleted adsorption separation unit 16 is mixed with the waste gas 49 of the cryogenic apparatus 21 and the The mixture is compressed in a compressor 22 to form a gaseous fuel 20.
  • the synthesis gas portion 12 may be mixed with the gaseous fuel 20.
  • synthesis gas 1 is no longer produced or is produced in a reduced quantity, below a threshold, at least the following three gases are recycled and downstream from the source of the synthesis gas and optionally upstream of the compressor 3:
  • the percentages of the recycled gases differ little to reconstitute the synthesis gas by mixing the different products 45, 51, 14.
  • a liquid carbon monoxide capacity 24 can be used within the distillation apparatus 21 and / or a carbon monoxide gas capacity 38 fed from the compressor 33 through line 36 to provide the missing carbon monoxide.
  • the liquid of the storage 24 is vaporized in the vaporizer 25.
  • valve 40 will be opened to supply carbon monoxide from storage 38 to the customer if synthesis gas 1 is missing.
  • recycling is carried out in the following manner.
  • a first step the flow of synthesis gas falls below a threshold or stops.
  • the synthesis gas is recycled from the storage 8 (or the pipe downstream of the compressor 3 if its volume and pressure allow it) upstream of the compressor 3.
  • This gas 2 can be natural gas from a pipe or a synthesis gas from another source.

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Abstract

In a method for separating a synthesis gas containing carbon monoxide and hydrogen, a synthesis gas (1) flow from a synthesis gas source is compressed in a compressor (3) and separated into at least three gaseous products. If there is insufficient synthesis gas, at least three separation products are recycled in the compressor in order to separate said products.

Description

Procédé et appareil de séparation d'un gaz de synthèse  Method and apparatus for separating a synthesis gas
La présente invention est relative à un procédé et à un appareil de séparation d'un gaz de synthèse. En particulier, le gaz de synthèse comprend du monoxyde de carbone et de l'hydrogène et éventuellement du méthane et/ou de l'azote The present invention relates to a method and apparatus for separating a synthesis gas. In particular, the synthesis gas comprises carbon monoxide and hydrogen and optionally methane and / or nitrogen
Un appareil de distillation cryogénique est alimenté en gaz de synthèse par d'une unité de génération de gaz de synthèse de type reformage ou/et oxydation partielle (SMR, ATR, POX, ...). Le gaz de synthèse en sortie de l'unité de génération est refroidi (pour la production de vapeur et divers préchauffes et éventuellement par de l'eau de refroidissement), puis envoyé vers un système d'extraction du CO2 (typiquement par lavage aux aminés tel que MEA, MDEA, aMDEA), puis séché avant d'être envoyé à l'appareil de distillation cryogénique pour séparation et purification du CO. Dans certains cas, notamment lorsque le gaz de synthèse est produit par une unité de génération par oxydation partielle produisant de l'acétylène, le gaz résiduaire dénommé AOG ou « acétylène offgas » en anglais constitue le gaz de synthèse. Il est comprimé avec un compresseur en amont de l'appareil de distillation cryogénique. La pression à laquelle ce gaz est comprimé est compatible avec la pression de produit riche en hydrogène requise. Ainsi, il n'est pas obligatoire de recomprimer l'hydrogène avant son transfert au client. A cryogenic distillation apparatus is supplied with synthesis gas by a synthesis gas generation unit such as reforming or / and partial oxidation (SMR, ATR, POX, ...). The synthesis gas at the output of the generation unit is cooled (for the production of steam and various preheaters and possibly by cooling water) and then sent to a CO 2 extraction system (typically by washing with amines such as MEA, MDEA, aMDEA) and then dried before being sent to the cryogenic distillation apparatus for CO separation and purification. In some cases, especially when the synthesis gas is produced by a partial oxidation generating unit producing acetylene, the residual gas called AOG or "acetylene offgas" in English is the synthesis gas. It is compressed with a compressor upstream of the cryogenic distillation apparatus. The pressure at which this gas is compressed is compatible with the hydrogen-rich product pressure required. Thus, it is not mandatory to recompress the hydrogen before it is transferred to the customer.
Généralement, quand l'unité qui consomme le CO est opérée à charge réduite, la partie de génération de gaz de synthèse ne délivre que les molécules de CO demandées (pour ne pas dégrader les coûts opératoires et d'éviter le plus possible de mettre à la torche des produits CO et/ou H2 excédentaires). L'appareil de distillation cryogénique va fonctionner à un faible régime, exprimé en rapport du débit de CO et/ou d'H2 sur les débits de charge nominaux. Ainsi, la stabilité de fonctionnement de l'appareil de distillation cryogénique à basse charge sur le long terme pose problème avec risques accrus de ne pas respecter la pureté demandée du CO ou d'avoir des débits de production trop fluctuants. Afin d'assurer un fonctionnement stable de l'appareil de distillation cryogénique, il est nécessaire de l'opérer avec un débit de charge suffisant qui peut être supérieur aux besoins ponctuels des clients. Les coûts opératoires sont dégradés du fait de devoir opérer l'appareil de distillation cryogénique à un niveau de charge supérieur aux besoins des clients. Generally, when the unit that consumes the CO is operated under reduced load, the synthesis gas generation part delivers only the requested CO molecules (in order not to degrade the operating costs and to avoid as much as possible to put in the torch of surplus CO and / or H2 products). The cryogenic distillation apparatus will operate at a low rate, expressed as a ratio of the flow rate of CO and / or H2 to the nominal flow rates. Thus, the operating stability of the cryogenic distillation apparatus at low load over the long term poses a problem with increased risks of not respecting the required purity of the CO or having too fluctuating production rates. In order to ensure a stable operation of the cryogenic distillation apparatus, it is necessary to operate it with a sufficient charge rate which may be greater than the specific needs of the customers. The costs The operations are degraded by having to operate the cryogenic distillation apparatus at a level of load higher than the needs of the customers.
Lorsque l'unité de génération de gaz de synthèse s'arrête intempestivement, cela conduit à arrêter l'appareil de distillation cryogénique qui n'est plus alimenté en molécules de gaz de synthèse. Une fois que le gaz de synthèse est à nouveau disponible, une certaine durée (de l'ordre de plusieurs heures) est requise pour redémarrer avant d'être en mesure de produire à nouveau du CO à la pureté requise.  When the synthesis gas generation unit stops unexpectedly, this leads to stopping the cryogenic distillation apparatus which is no longer supplied with synthesis gas molecules. Once the synthesis gas is available again, a certain duration (of the order of hours) is required to restart before being able to produce CO again at the required purity.
Ainsi, une coupure de quelques minutes sur l'unité de génération du gaz de synthèse entraîne une rupture de production de CO pendant plusieurs heures. Les clients en aval devront donc à leur tour arrêter leurs installations consommatrices de CO qui à leur tour devront être redémarrées.  Thus, a break of a few minutes on the synthesis gas generation unit causes a break in CO production for several hours. Downstream customers will need to shut down their CO consuming facilities, which in turn will need to be restarted.
La solution technique présentée ci-après permet donc d'empêcher des arrêts longs d'une installation industrielle engendrant des coûts élevés de non-production :1e recyclage des fluides produits par l'appareil de distillation cryogénique à l'entrée de cet appareil (fonctionnant par exemple par lavage au méthane et/ou condensation partielle et/ou lavage au monoxyde de carbone) lors d'un fonctionnement à marche réduite ou lors d'arrêt de l'unité qui génère le gaz de synthèse.  The technical solution presented below thus makes it possible to prevent long shutdowns of an industrial installation generating high costs of non-production: recycling of the fluids produced by the cryogenic distillation apparatus at the inlet of this apparatus (operating for example by washing with methane and / or partial condensation and / or washing with carbon monoxide) during a reduced running operation or when stopping the unit that generates the synthesis gas.
Lors de la production de monoxyde de carbone et d'hydrogène à partir d'un gaz de synthèse généré par reformage ou oxydation partielle, on utilise généralement un appareil de distillation cryogénique et une unité d'adsorption. L'appareil de distillation cryogénique assure la purification du CO et la production d'un débit enrichi en hydrogène qui est ensuite épuré en hydrogène par adsorption.  In the production of carbon monoxide and hydrogen from a synthesis gas generated by reforming or partial oxidation, a cryogenic distillation apparatus and an adsorption unit are generally used. The cryogenic distillation apparatus purifies the CO and produces a hydrogen enriched flow which is then purified to hydrogen by adsorption.
La solution proposée est de recycler des gaz produits par l'appareil de distillation cryogénique, éventuellement tous les gaz produits par l'appareil de distillation cryogénique, en amont de l'appareil de distillation cryogénique. Ainsi, les unités de séparation ne sont pas arrêtées et lorsque la source génératrice de gaz de synthèse revient en opération, il devient possible de traiter à nouveau le gaz de synthèse et de produire les produits requis. Cette solution permet également d'assurer des descentes en charge jusqu'à 0% de la source sans arrêt au lieu de 40% typiquement.  The proposed solution is to recycle gases produced by the cryogenic distillation apparatus, possibly all the gases produced by the cryogenic distillation apparatus, upstream of the cryogenic distillation apparatus. Thus, the separation units are not stopped and when the synthesis gas generating source returns to operation, it becomes possible to reprocess the synthesis gas and produce the required products. This solution also makes it possible to ensure descending loads of up to 0% of the source without stopping instead of typically 40%.
Selon un objet de l'invention, il est prévu un procédé de séparation d'un gaz de synthèse contenant du monoxyde de carbone et de l'hydrogène dans lequel : i) on comprime un débit de gaz de synthèse provenant d'une source de gaz de synthèse dans un compresseur According to one object of the invention, there is provided a process for separating a synthesis gas containing carbon monoxide and hydrogen in which: i) compressing a flow of synthesis gas from a source of synthesis gas into a compressor
ii) on purifie le gaz de synthèse comprimé dans une unité de purification pour l'épurer en eau et en dioxyde de carbone  ii) purifying the compressed synthesis gas in a purification unit to purify it with water and carbon dioxide
iii) on refroidit le débit de gaz de synthèse comprimé et purifié  iii) the flow of compressed and purified synthesis gas is cooled
iv) on sépare le débit de gaz de synthèse refroidi par lavage et/ou distillation à une température cryogénique et éventuellement par adsorption dans une unité de séparation et  iv) the cooled synthesis gas flow is separated by washing and / or distillation at a cryogenic temperature and optionally by adsorption in a separation unit and
v) on produit dans l'unité de séparation au moins les trois gaz suivants : un gaz enrichi en monoxyde de carbone, un gaz enrichi en hydrogène, un gaz résiduaire contenant du monoxyde de carbone et de l'hydrogène moins pur en monoxyde de carbone que le gaz enrichi en monoxyde de carbone et moins pur en hydrogène que le gaz enrichi en hydrogène et éventuellement aussi un gaz enrichi en méthane, et/ou un gaz enrichi en azote caractérisé en ce qu'uniquement si le débit de gaz de synthèse envoyé au compresseur est inférieur à un seuil ou nul, on envoie au moins une partie d'au moins deux, voire de chacun des trois gaz suivants :1e gaz enrichi en monoxyde de carbone, le gaz enrichi en hydrogène et le gaz résiduaire contenant du monoxyde de carbone et de l'hydrogène en aval de la source, et éventuellement en amont du compresseur, pour être purifiés dans l'unité de purification et séparés dans l'unité de séparation.  v) at least the following three gases are produced in the separation unit: a carbon monoxide enriched gas, a hydrogen enriched gas, a carbon monoxide containing waste gas and a less pure carbon monoxide gas that the gas enriched in carbon monoxide and less pure hydrogen than the gas enriched in hydrogen and optionally also a gas enriched in methane, and / or a nitrogen-enriched gas characterized in that only if the flow of synthesis gas sent at the compressor is below a threshold or zero, at least a portion of at least two or even of each of the following three gases is sent: the carbon monoxide enriched gas, the hydrogen enriched gas and the monoxide-containing waste gas carbon and hydrogen downstream of the source, and possibly upstream of the compressor, to be purified in the purification unit and separated in the separation unit.
Selon un autre aspect de l'invention dans le procédé :  According to another aspect of the invention in the process:
a) on stocke du gaz de synthèse comprimé pendant que le débit de gaz de synthèse est supérieur au seuil et  a) compressed synthesis gas is stored while the synthesis gas flow rate is above the threshold and
b) on envoie au moins une partie du gaz de synthèse comprimé ainsi qu'au moins une partie d'au moins chacun des trois premiers gaz de l'étape v) en aval de la source, et éventuellement en amont du compresseur, pour être purifiée dans l'unité de purification et séparés dans l'unité de séparation.  b) at least a portion of the compressed synthesis gas and at least a part of at least each of the first three gases of step v) downstream of the source, and possibly upstream of the compressor, are sent to be purified in the purification unit and separated in the separation unit.
Selon d'autres aspects facultatifs de l'invention :  According to other optional aspects of the invention:
au moins une partie d'au moins chacun des trois premiers gaz de l'étape v) en aval de la source et éventuellement en amont du compresseur uniquement si le débit de gaz de synthèse est inférieur au seuil, voire si aucun débit ne provient de la source. pendant le fonctionnement nominal du procédé, les productions de l'unité de séparations sont des productions nominales at least a part of at least each of the first three gases of step v) downstream of the source and possibly upstream of the compressor only if the flow rate of synthesis gas is below the threshold, or if no flow comes from source. during the nominal operation of the process, the outputs of the separation unit are nominal productions
on envoie  we send
i) x% de la production nominale du gaz enrichi en monoxyde de carbone et y% de la production nominale du gaz enrichi en hydrogène à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, x et y différant d'au plus 5% et/ou  i) x% of the nominal production of the carbon monoxide enriched gas and y% of the nominal production of the hydrogen enriched gas at the separation unit (16, 21, 41) when the syngas flow is below a threshold, x and y differing by not more than 5% and / or
ii°) y% de la production nominale du gaz enrichi en hydrogène et z% de la production nominale du gaz résiduaire à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, y et z différant d'au plus 5% et/ou  (ii) y% of the nominal production of the hydrogen-enriched gas and z% of the nominal production of the waste gas at the separation unit (16, 21, 41) when the synthesis gas flow rate is below one threshold, y and z differing by not more than 5% and / or
iii) x% de la production nominale du gaz enrichi en monoxyde de carbone et z% de la production nominale du gaz résiduaire à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, x et z différant d'au plus 5%  (iii) x% of the nominal production of the carbon monoxide enriched gas and z% of the nominal production of the residual gas at the separation unit (16, 21, 41) when the synthesis gas flow rate is below a threshold, x and z differing by not more than 5%
- on envoie seulement x% de la production nominale du gaz enrichi en monoxyde de carbone, y% de la production nominale du gaz enrichi en hydrogène et z% de la production nominale du gaz résiduaire à l'unité de séparation quand le débit de gaz de synthèse est en dessous d'un seuil, x, y et z différant d'au plus 5% .  - only x% of the nominal production of the carbon monoxide-enriched gas, y% of the nominal production of the hydrogen enriched gas and z% of the nominal production of the waste gas to the separation unit are sent when the gas flow rate is below a threshold, x, y and z differing by at most 5%.
on stocke une partie du gaz enrichi en monoxyde de carbone dans un stockage  some of the carbon monoxide enriched gas is stored in a storage
et on envoie le reste du gaz enrichi en monoxyde de carbone à un client si le débit de gaz de synthèse est supérieur au seuil et on envoie du gaz enrichi en monoxyde de carbone provenant du stockage au client si le débit de gaz de synthèse est inférieur au seuil.  and the remaining carbon monoxide enriched gas is sent to a customer if the synthesis gas flow rate is above the threshold and carbon monoxide enriched gas from the storage is sent to the customer if the synthesis gas flow rate is lower than the threshold. threshold.
- si le débit de gaz de synthèse est inférieur au seuil, tout le gaz enrichi en monoxyde de carbone envoyé au client provient du stockage et éventuellement tout le gaz enrichi en monoxyde de carbone provenant directement de l'unité de séparation sans passer pas le stockage est envoyé en amont du compresseur et en aval de la source.  - if the synthesis gas flow rate is below the threshold, all the carbon monoxide enriched gas sent to the customer comes from the storage and possibly all the carbon monoxide enriched gas coming directly from the separation unit without passing the storage is sent upstream of the compressor and downstream of the source.
- le gaz de synthèse est un gaz résiduaire d'une unité de production d'acétylène. si le débit de gaz de synthèse est supérieur au seuil, on stocke une partie du gaz de synthèse dans un stockage et si le débit de gaz de synthèse est inférieur au seuil, on envoie du gaz de synthèse du stockage vers le compresseur. the synthesis gas is a waste gas from an acetylene production unit. if the flow rate of synthesis gas is greater than the threshold, a part of the synthesis gas is stored in a storage and if the flow rate of synthesis gas is below the threshold, synthesis gas is sent from the storage to the compressor.
si le débit de gaz de synthèse est nul, l'unité de séparation est alimentée uniquement par des gaz produits par l'unité de séparation.  if the flow rate of synthesis gas is zero, the separation unit is fed solely by gases produced by the separation unit.
on comprime le gaz enrichi en monoxyde de carbone dans un compresseur de produit et on l'envoie au client et si le débit de gaz de synthèse est inférieur au seuil et le débit de gaz enrichi en monoxyde de carbone à comprimer est inférieur à un autre seuil, on envoie de l'azote gazeux au compresseur de produit pour être comprimé avec le gaz enrichi en monoxyde de carbone.  the carbon monoxide enriched gas is compressed in a product compressor and sent to the customer and if the synthesis gas flow rate is below the threshold and the carbon monoxide enriched gas flow rate to be compressed is less than another At the threshold, nitrogen gas is sent to the product compressor to be compressed with the carbon monoxide enriched gas.
si le débit de gaz de synthèse est inférieur à un seuil, on envoie un gaz riche en un composant du gaz de synthèse provenant d'une autre source qui n'est pas l'appareil de séparation à l'unité de séparation.  if the synthesis gas flow rate is below a threshold, a rich gas is sent to a synthesis gas component from another source that is not the separation apparatus to the separation unit.
le gaz enrichi en monoxyde de carbone est comprimé dans un compresseur, ensuite divisé en deux, une partie comprimée servant de produit et une partie comprimée étant recyclé en aval de la source et/ou le gaz enrichi en hydrogène est comprimé dans un compresseur, ensuite divisé en deux, une partie comprimée servant de produit et une partie comprimée étant recyclé en aval de la source .  the carbon monoxide enriched gas is compressed in a compressor, then divided into two, a compressed portion serving as a product and a compressed portion being recycled downstream of the source and / or the hydrogen-enriched gas is compressed in a compressor, then divided in two, a compressed portion serving as a product and a compressed portion being recycled downstream of the source.
Selon un autre objet de l'invention, il est prévu un appareil de séparation d'un gaz de synthèse contenant du monoxyde de carbone et de l'hydrogène comprenant un compresseur pour comprimer un débit de gaz de synthèse provenant d'une source de gaz de synthèse , une unité de purification pour épurer en eau et/ou en dioxyde de carbone le gaz de synthèse comprimé, des moyens pour refroidir le débit de gaz de synthèse comprimé et purifié, une unité de séparation du débit de gaz de synthèse refroidi par lavage et/ou distillation à une température cryogénique comprenant éventuellement une unité d'adsorption, des moyens pour produire de l'unité de séparation au moins les trois gaz suivants : un gaz enrichi en monoxyde de carbone, un gaz enrichi en hydrogène , un gaz résiduaire contenant du monoxyde de carbone et de l'hydrogène moins pur en monoxyde de carbone que le gaz enrichi en monoxyde de carbone et moins pur en hydrogène que le gaz enrichi en hydrogène et éventuellement aussi un gaz enrichi en méthane, et/ou un gaz enrichi en azote, des moyens pour envoyer au moins une partie d'au moins deux , voire de chacun des trois gaz suivants :le gaz enrichi en monoxyde de carbone, le gaz enrichi en hydrogène et le gaz résiduaire contenant du monoxyde de carbone et de l'hydrogène en aval de la source, et éventuellement en amont du compresseur, pour être purifiés dans l'unité de purification et séparés dans l'unité de séparation et des moyens pour déclencher le renvoi d'au moins une partie des au moins deux gaz en fonction du débit de gaz de synthèse provenant de la source en amont du compresseur. According to another object of the invention, there is provided an apparatus for separating a synthesis gas containing carbon monoxide and hydrogen comprising a compressor for compressing a flow of synthesis gas from a gas source. of synthesis, a purification unit for purifying the compressed synthesis gas, water, and / or carbon dioxide, means for cooling the compressed and purified synthesis gas flow, a separation unit of the synthesis gas flow cooled by washing and / or distillation at a cryogenic temperature optionally comprising an adsorption unit, means for producing separation unit at least the following three gases: a gas enriched in carbon monoxide, a gas enriched in hydrogen, a gas carbon monoxide and hydrogen less pure carbon monoxide than the carbon monoxide enriched and less pure hydrogen gas than the hydrogen enriched gas and optionally also a gas enriched in methane, and / or a gas enriched in nitrogen, means for sending at least a portion of at least two or even of each of the three gases carbon monoxide enriched gas, the hydrogen-enriched gas and the carbon monoxide and hydrogen-containing tail gas downstream of the source, and possibly upstream of the compressor, to be purified in the unit of purification and separated in the separation unit and means for triggering the return of at least a portion of the at least two gases depending on the flow of synthesis gas from the source upstream of the compressor.
Selon d'autres aspects facultatifs, l'appareil comprend :  According to other optional aspects, the apparatus comprises:
- un stockage en aval du compresseur et en amont de l'unité de purification ce stockage étant relié à la conduite d'entrée du compresseur par des moyens ne transitant pas par le compresseur.  a storage downstream of the compressor and upstream of the purification unit, this storage being connected to the inlet duct of the compressor by means not passing through the compressor.
- des moyens pour envoyer du gaz du stockage en amont du compresseur en fonction du débit de gaz de synthèse provenant de la source en amont du compresseur means for sending gas from the storage upstream of the compressor as a function of the flow rate of synthesis gas coming from the source upstream of the compressor
En particulier, dans le cas où le gaz de synthèse est comprimé en amont de l'appareil de distillation cryogénique par un compresseur (comme par exemple lorsque le gaz de synthèse est constitué d'un flux de résiduaire (le dénommé « Acétylène Offgas ») d'une unité produisant de l'acétylène), on utilise le compresseur de gaz de synthèse pour recycler les fluides produits par l'appareil de distillation cryogénique afin de : In particular, in the case where the synthesis gas is compressed upstream of the cryogenic distillation apparatus by a compressor (as for example when the synthesis gas consists of a waste stream (the so-called "Acetylene Offgas") of a unit producing acetylene), the synthesis gas compressor is used to recycle the fluids produced by the cryogenic distillation apparatus in order to:
1) Maintenir un débit suffisant vers l'appareil de distillation cryogénique en complément du débit de gaz de synthèse produit par l'unité amont et être en mesure de produire un débit de CO inférieur au minimum technique de l'appareil de distillation cryogénique.  1) Maintain a sufficient flow rate to the cryogenic distillation apparatus in addition to the flow of synthesis gas produced by the upstream unit and be able to produce a flow of CO below the technical minimum of the cryogenic distillation apparatus.
2) Maintenir l'appareil de distillation cryogénique en fonctionnement y compris lors d'arrêt de l'unité produisant le gaz de synthèse, dans ce cas l'appareil de distillation cryogénique sera alimentée uniquement par les gaz recyclés, le temps que le gaz de synthèse produit par l'unité en amont soit à nouveau disponible.  2) Keeping the cryogenic distillation apparatus in operation, even when the unit producing the synthesis gas is stopped, in this case the cryogenic distillation apparatus will be fed solely by the recycled gases, whereas the gas of synthesis produced by the upstream unit is available again.
- Afin d'assurer la fourniture du client en CO pendant le temps où le gaz de synthèse n'est pas disponible on ajoutera un stockage liquide de molécules de CO dans l'appareil de distillation cryogénique. Ce CO sera vaporisé pendant la durée de coupure d'alimentation de l'appareil de distillation cryogénique.  - In order to ensure the customer's supply of CO during the time when the synthesis gas is not available, a liquid storage of CO molecules in the cryogenic distillation apparatus will be added. This CO will be vaporized during the power cut-off time of the cryogenic distillation apparatus.
Pour compenser le temps de démarrage de la vaporisation, on pourra ajouter une capacité tampon de CO gazeux. En effet, les gaz produits par l'appareil de distillation cryogénique seront alors recyclés et le gaz requis par le client proviendra alors de cette capacité tampon installée en amont de la vanne de contrôle sur la ligne de production de CO et sera opérée à une pression supérieure à la pression requise par l'unité qui consomme le CO. To compensate for the start time of the vaporization, a buffer capacity of CO gas may be added. Indeed, the gases produced by the apparatus of Cryogenic distillation will then be recycled and the gas required by the customer will then come from this buffer capacity installed upstream of the control valve on the CO production line and will be operated at a pressure greater than the pressure required by the unit that consumes the CO.
- Pour compenser le temps de l'ouverture des vannes des tuyaux de recyclage, on pourra ajouter une capacité tampon à haute pression qui sera alimentée par la sortie du compresseur d'AOG et qui sera connectée à l'aspiration du compresseur. . Cette capacité tampon pourra donc compenser les premières secondes du cas transitoire de fermeture de la vanne et également les très légères fuites au niveau du compresseur et/ou du système d'extraction du CO2.  - To compensate for the time of the opening of the valves of the recycling pipes, we can add a high pressure buffer capacity which will be fed by the output of the AOG compressor and which will be connected to the suction of the compressor. . This buffer capacity can therefore compensate for the first seconds of the transient case of closure of the valve and also the very slight leaks at the compressor and / or the CO2 extraction system.
De l'azote pourra éventuellement être injecté à l'aspiration du compresseur de CO pour contrebalancer les fuites au niveau du compresseur. On préférera  Nitrogen may be injected at the CO compressor suction to counterbalance compressor leakage. We will prefer
néanmoins compenser les pertes du compresseur de CO par l'appoint de molécules extérieures provenant d'une capacité tampon de CO gazeux de la capacité liquide de CO. nevertheless, to compensate the losses of the CO compressor by the addition of external molecules originating from a CO gas buffer capacity of the liquid CO capacity.
En effet, ajouter de l'azote dégrade la qualité du CO produit  In fact, adding nitrogen degrades the quality of the CO produced
Ces idées combinées permettent de toujours maintenir un débit de production de CO vers le client y compris lors d'arrêt de courte durée de l'unité de génération de gaz de synthèse et apporte ainsi une fiabilisation de l'installation pour le client final en lissant les coupures de fournitures de l'installation de génération de gaz de synthèse.  These combined ideas make it possible to always maintain a rate of production of CO towards the customer, including during a short-term shutdown of the synthesis gas generation unit, and thus make the installation more reliable for the end customer by smoothing supply cuts in the syngas generation facility.
L'invention sera décrite en plus de détail en se référant aux Figures 1 à 3 qui représentent des procédés selon l'invention.  The invention will be described in more detail with reference to Figures 1 to 3 which show methods according to the invention.
Dans la Figure 1 , un gaz de synthèse 1 provient d'une unité de génération de gaz de synthèse, par exemple, une unité de reformage, tel qu'un SMR ou un ATR ou une unité d'oxydation partielle, qui produit par exemple de l'acétylène. Le gaz de synthèse 1 contient du monoxyde de carbone, du dioxyde de carbone, de l'hydrogène et éventuellement du méthane et de l'azote.  In FIG. 1, a synthesis gas 1 comes from a synthesis gas generation unit, for example, a reforming unit, such as an SMR or an ATR or a partial oxidation unit, which produces, for example acetylene. The synthesis gas 1 contains carbon monoxide, carbon dioxide, hydrogen and optionally methane and nitrogen.
Le gaz 1 est comprimé par un compresseur 3 pour former un gaz comprimé 5. Le gaz comprimé 5 est envoyé dans une unité de traitement 7 par hydrogénation pour enlever l'oxygène et les hydrocarbures insaturés en produisant un débit 9. Le débit 9 est envoyé à une unité d'épuration en CO2 13, par exemple par lavage aux aminés produisant un débit de purge riche en CO2 1 1 et un débit de gaz de synthèse appauvri en C02 15. Le débit 15 est envoyé à une unité d'épuration en C02 par adsorption 17 pour enlevant le C02 restant. Le gaz de synthèse épuré en C02 19 est envoyé à une unité de distillation cryogénique 21 où le gaz de synthèse est refroidi et puis séparé dans au moins une colonne de distillation, comprenant par exemple une étape de lavage au méthane et/ou condensation partielle et/ou lavage au monoxyde de carbone. L'unité de distillation cryogénique 21 produit un débit gazeux enrichi en monoxyde de carbone 26, un gaz riche en hydrogène 27 et un gaz résiduaire 23 contenant du monoxyde de carbone et de l'hydrogène, moins pur en monoxyde de carbone que le gaz 26 et moins pur en hydrogène que le gaz 27. Le débit gazeux enrichi en monoxyde de carbone 26 est comprimé dans un compresseur 33. Un débit gazeux 31 venant de la sortie du compresseur 33 est renvoyé à l'unité de distillation cryogénique 21. Le débit 37 représente des pertes des gaz enrichi en monoxyde de carbone du compresseur 33. Le gaz venant d'un étage intermédiaire du compresseur 33 forme en partie 39 un produit. The gas 1 is compressed by a compressor 3 to form a compressed gas 5. The compressed gas 5 is sent to a treatment unit 7 by hydrogenation to remove oxygen and unsaturated hydrocarbons producing a flow rate 9. The flow 9 is sent to a CO2 purification unit 13, for example by washing with amines producing a purge flow rich in CO2 1 1 and a depleted synthesis gas flow rate The flow rate 15 is fed to an adsorption CO 2 purification unit 17 to remove the remaining CO 2. The CO2 purified synthesis gas 19 is sent to a cryogenic distillation unit 21 where the synthesis gas is cooled and then separated in at least one distillation column, comprising for example a methane washing step and / or partial condensation and / or carbon monoxide wash. The cryogenic distillation unit 21 produces a gas flow enriched in carbon monoxide 26, a gas rich in hydrogen 27 and a waste gas 23 containing carbon monoxide and hydrogen, less pure carbon monoxide than the gas 26 and less pure hydrogen than gas 27. The carbon monoxide enriched gas stream 26 is compressed in a compressor 33. A gas flow 31 from the outlet of the compressor 33 is returned to the cryogenic distillation unit 21. 37 shows losses of the carbon monoxide enriched gas from the compressor 33. The gas from an intermediate stage of the compressor 33 partially forms a product.
Si le débit de gaz de synthèse provenant de la source de gaz de synthèse est nul, la totalité de ces trois produits 23, 27 ,39 est renvoyée à la purification. L'hydrogène et le gaz résiduaire doivent être comprimés dans le compresseur 3 mais le monoxyde de carbone peut être comprimé à la pression requise dans le compresseur 33 et recyclé en aval du compresseur 3. Ainsi les gaz 23 et 27 doivent être envoyé en amont du compresseur 3 alors que le gaz 26 peut être recyclé en amont ou en aval du compresseur 3.  If the flow rate of synthesis gas from the synthesis gas source is zero, all of these three products 23, 27, 39 are returned to the purification. The hydrogen and the waste gas must be compressed in the compressor 3 but the carbon monoxide can be compressed to the pressure required in the compressor 33 and recycled downstream of the compressor 3. Thus the gases 23 and 27 must be sent upstream of the compressor. compressor 3 while the gas 26 can be recycled upstream or downstream of the compressor 3.
Pendant le fonctionnement nominal du procédé, les productions de l'unité de séparations sont des productions nominales  During the nominal operation of the process, the outputs of the separation unit are nominal productions
En fonctionnement avec production de gaz de synthèse basse ou nulle, on envoie  In operation with production of low or zero synthesis gas, it sends
i) x% de la production nominale du gaz enrichi en monoxyde de carbone et y% de la production nominale du gaz enrichi en hydrogène à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, x et y différant d'au plus 5% et/ou ii°) y% de la production nominale du gaz enrichi en hydrogène et z% de la production nominale du gaz résiduaire à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, y et z différant d'au plus 5% et/ou iii). x% de la production nominale du gaz enrichi en monoxyde de carbone et z% de la production nominale du gaz résiduaire à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, x et z différant d'au plus 5%. i) x% of the nominal production of the carbon monoxide enriched gas and y% of the nominal production of the hydrogen enriched gas at the separation unit (16, 21, 41) when the syngas flow is below of a threshold, x and y differing by not more than 5% and / or ii °) y% of the nominal production of the hydrogen-enriched gas and z% of the nominal production of the residual gas at the separation unit (16 , 21, 41) when the synthesis gas flow rate is below a threshold, y and z differ by at most 5% and / or iii). x% of the nominal production of the carbon monoxide enriched gas and z% of the nominal production of the residual gas at the separation unit (16, 21, 41) when the synthesis gas flow is below a threshold , x and z differ by not more than 5%.
Par exemple, si le débit de gaz de synthèse n'est pas nul mais est inférieur à un seuil, un pourcentage de x% du gaz riche en monoxyde de carbone, y% du gaz riche en hydrogène et z% du gaz résiduaire peuvent être renvoyés à l'unité de purification et ensuite à la séparation cryogénique. Les pourcentages x, y and z sont de préférence identiques mais peuvent différer de moins de 5%.  For example, if the synthesis gas flow rate is not zero but is below a threshold, a percentage of x% of the carbon monoxide-rich gas, y% of the hydrogen-rich gas and z% of the waste gas may be returned to the purification unit and then to the cryogenic separation. The percentages x, y and z are preferably the same but may differ by less than 5%.
Quand au moins une partie du monoxyde de carbone du compresseur 33 est recyclée, on peut injecter de l'azote gazeux 35 à un niveau intermédiaire ou à l'aspiration du compresseur 33 pour compenser les fuites du compresseur.  When at least a portion of the carbon monoxide of the compressor 33 is recycled, nitrogen gas can be injected at an intermediate level or at the suction of the compressor 33 to compensate for compressor leakage.
La Figure 2 diffère de la Figure 1 en ce que le débit 30 enrichi en hydrogène est envoyé de l'unité 17 d'adsorption qui enlève l'eau et le C02 à un appareil de purification par adsorption 41. Cet appareil 41 produit un gaz riche en hydrogène 43. Le gaz appauvri en hydrogène 47 venant de l'appareil 41 est mélangé avec le résiduaire 49 de l'appareil 21 et comprimé dans un compresseur 53 pour fournir un gaz résiduaire sous pression.  Figure 2 differs from Figure 1 in that the hydrogen enriched flow is fed from the adsorption unit 17 which removes water and CO 2 to an adsorption purification apparatus 41. This apparatus 41 produces a gas. The hydrogen-depleted gas 47 from the apparatus 41 is mixed with the waste 49 of the apparatus 21 and compressed in a compressor 53 to provide a pressurized waste gas.
Ainsi si le gaz de synthèse 1 n'est plus produit ou est produit en quantité réduite, on recycle au moins certains produits de l'appareil de distillation cryogénique 21 en amont du compresseur 3, éventuellement après une étape supplémentaire de traitement. En plus du reste 51 du gaz de l'étage intermédiaire du compresseur 33 ou à la place du gaz 51 , on peut recycler en amont du compresseur 3 au moins une partie 45 du produit riche en hydrogène 43 et/ou au moins une partie 55 du gaz résiduaire provenant du compresseur 53.  Thus, if the synthesis gas 1 is no longer produced or is produced in a reduced amount, at least some products of the cryogenic distillation apparatus 21 are recycled upstream of the compressor 3, possibly after an additional treatment step. In addition to the remainder 51 of the gas of the intermediate stage of the compressor 33 or instead of the gas 51, at least a portion 45 of the hydrogen-rich product 43 and / or at least a portion of the hydrogen-rich product 43 can be recycled upstream of the compressor 3 waste gas from the compressor 53.
La Figure 3 diffère de la Figure 1 en ce qu'une partie 4 du gaz de synthèse est prise à une pression intermédiaire du compresseur 3 pour la partie 4 et à la pression finale de celui-ci pour la partie 4 et ne sont pas traitées dans les unités 7,13,17,21. La partie 4 est envoyée de la pression finale du compresseur 3 à une unité de séparation par adsorption appelée PSA 16 où elle est épurée pour former un débit riche en hydrogène 52. Le résiduaire 18 de l'unité de séparation par adsorption 16 appauvri en hydrogène est mélangé avec le gaz 49 résiduaire de l'appareil cryogénique 21 et le mélange est comprimé dans un compresseur 22 pour former un carburant gazeux 20. La partie 12 de gaz de synthèse peut être mélangée avec le carburant gazeux 20. FIG. 3 differs from FIG. 1 in that part 4 of synthesis gas is taken at an intermediate pressure of compressor 3 for part 4 and at the final pressure thereof for part 4 and is not treated. in units 7,13,17,21. Part 4 is sent from the final pressure of the compressor 3 to an adsorption separation unit called PSA 16 where it is purified to form a hydrogen-rich flow 52. The waste 18 of the hydrogen-depleted adsorption separation unit 16 is mixed with the waste gas 49 of the cryogenic apparatus 21 and the The mixture is compressed in a compressor 22 to form a gaseous fuel 20. The synthesis gas portion 12 may be mixed with the gaseous fuel 20.
Si le gaz de synthèse 1 n'est plus produit ou est produit en quantité réduite, en dessous d'un seuil, on recycle au moins les trois gaz suivants et en aval de la source du gaz de synthèse et éventuellement vers l'amont du compresseur 3:  If the synthesis gas 1 is no longer produced or is produced in a reduced quantity, below a threshold, at least the following three gases are recycled and downstream from the source of the synthesis gas and optionally upstream of the compressor 3:
i) Au moins une partie 51 du gaz enrichi en monoxyde de carbone 39 provenant de l'appareil de distillation cryogénique 21  i) At least a portion 51 of the carbon monoxide enriched gas 39 from the cryogenic distillation apparatus 21
ii) Au moins une partie 45 du gaz enrichi en hydrogène provenant de l'unité de séparation par adsorption 16  ii) At least a portion 45 of the hydrogen-enriched gas from the adsorption separation unit 16
iii) Au moins une partie 14 d'un gaz résiduaire contenant de l'hydrogène et/ou du monoxyde de carbone provenant de l'appareil de distillation cryogénique et/ou de l'unité de séparation par adsorption 16, moins pur en monoxyde de carbone que le gaz 51 et moins pur en hydrogène que le gaz 45 et éventuellement aussi  iii) at least a portion 14 of a waste gas containing hydrogen and / or carbon monoxide from the cryogenic distillation apparatus and / or the adsorption separation unit 16, less pure in carbon monoxide; carbon than gas 51 and less pure hydrogen than gas 45 and possibly also
iv) Une partie 6 du gaz de synthèse comprimé prise en aval du compresseur 3, stockée dans un stockage 8 pendant que le débit de gaz de synthèse est supérieur au seuil et renvoyée via la conduite 10 et une vanne.  iv) A portion 6 of the compressed synthesis gas taken downstream of the compressor 3, stored in a storage 8 while the flow rate of synthesis gas is greater than the threshold and returned via the pipe 10 and a valve.
De préférence les pourcentages des gaz recyclés diffèrent peu pour reconstituer le gaz de synthèse en mélangeant les différents produits 45, 51 , 14.  Preferably the percentages of the recycled gases differ little to reconstitute the synthesis gas by mixing the different products 45, 51, 14.
Afin de s'assurer qu'il y a suffisamment de monoxyde de carbone pour le client, on peut utiliser une capacité de monoxyde de carbone liquide 24 au sein de l'appareil de distillation 21 et/ou une capacité de monoxyde de carbone gazeux 38 alimentée à partir du compresseur 33 par la conduite 36 pour fournir le monoxyde de carbone qui manque. Le liquide du stockage 24 est vaporisé dans le vaporiseur 25.  In order to ensure that there is sufficient carbon monoxide for the customer, a liquid carbon monoxide capacity 24 can be used within the distillation apparatus 21 and / or a carbon monoxide gas capacity 38 fed from the compressor 33 through line 36 to provide the missing carbon monoxide. The liquid of the storage 24 is vaporized in the vaporizer 25.
En particulier, si une grande partie ou tout le monoxyde de carbone produit en temps réel est destiné au recyclage, le monoxyde de carbone stocké dans les capacités 24 ou 38 peut permettre d'alimenter le client. Ainsi par exemple on ouvrira la vanne 40 pour fournir du monoxyde de carbone du stockage 38 vers le client si le gaz de synthèse 1 vient à manquer.  In particular, if a large part or all carbon monoxide produced in real time is for recycling, the carbon monoxide stored in the 24 or 38 capacity can be used to supply the customer. Thus, for example, valve 40 will be opened to supply carbon monoxide from storage 38 to the customer if synthesis gas 1 is missing.
Dans une variante préférée, qui peut être utilisée sur tous les procédés des Figures 1 à 3 en utilisant le conduites présente ou en rajoutant les stockages requis, le recyclage est effectué de la manière suivante. Dans un premier temps, le débit de gaz de synthèse tombe en dessous d'un seuil ou s'arrête. Tout d'abord, on commence à ouvrir des vannes de recyclage sur au moins deux fluides produits en traitant le gaz de synthèse. Le gaz de synthèse est recyclé du stockage 8 (ou de la conduite en aval du compresseur 3 si son volume et sa pression le permettent) vers l'amont du compresseur 3. Une fois que les vannes de recyclage sont ouvertes, on recycle au moins les trois gaz suivants et en aval de la source du gaz de synthèse et éventuellement vers l'amont du compresseur 3: In a preferred variant, which can be used on all the processes of FIGS. 1 to 3 using the present lines or by adding the required storages, recycling is carried out in the following manner. In a first step, the flow of synthesis gas falls below a threshold or stops. First, we begin to open recycling valves on at least two fluids produced by treating the synthesis gas. The synthesis gas is recycled from the storage 8 (or the pipe downstream of the compressor 3 if its volume and pressure allow it) upstream of the compressor 3. Once the recycling valves are open, at least one recycle the following three gases and downstream of the source of the synthesis gas and possibly upstream of the compressor 3:
i) Au moins une partie 51 du gaz enrichi en monoxyde de carbone 39 provenant de l'appareil de distillation cryogénique 21  i) At least a portion 51 of the carbon monoxide enriched gas 39 from the cryogenic distillation apparatus 21
ii) Au moins une partie 45 du gaz enrichi en hydrogène provenant de l'unité de séparation par adsorption 16  ii) At least a portion 45 of the hydrogen-enriched gas from the adsorption separation unit 16
iii) Au moins une partie 14 d'un gaz résiduaire contenant de l'hydrogène et/ou du monoxyde de carbone provenant de l'appareil de distillation cryogénique et/ou de l'unité de séparation par adsorption 16, moins pur en monoxyde de carbone que le gaz 51 et moins pur en hydrogène que le gaz 45 et éventuellement aussi  iii) at least a portion 14 of a waste gas containing hydrogen and / or carbon monoxide from the cryogenic distillation apparatus and / or the adsorption separation unit 16, less pure in carbon monoxide; carbon than gas 51 and less pure hydrogen than gas 45 and possibly also
iv) Une partie 6 du gaz de synthèse comprimé prise en aval du compresseur 3, stockée dans un stockage 8 pendant que le débit de gaz de synthèse est supérieur au seuil et renvoyée via la conduite 10 et une vanne.  iv) A portion 6 of the compressed synthesis gas taken downstream of the compressor 3, stored in a storage 8 while the flow rate of synthesis gas is greater than the threshold and returned via the pipe 10 and a valve.
Dans certains cas, toute la production de l'appareil de séparation constitué par l'appareil de séparation par lavage et/ou distillation et éventuellement par l'unité d'adsorption est recyclée en amont du compresseur de gaz de synthèse.  In some cases, all the production of the separation apparatus consisting of the washing and / or distillation separation apparatus and possibly the adsorption unit is recycled upstream of the synthesis gas compressor.
Il est également possible pour toutes les figures de recycler le gaz enrichi en monoxyde de carbone 51 en aval du compresseur de gaz de synthèse 3. Le gaz 51 peut dans ce cas être pris à la pression de sortie du compresseur 3.  It is also possible for all the figures to recycle the carbon monoxide enriched gas 51 downstream of the synthesis gas compressor 3. The gas 51 can in this case be taken at the outlet pressure of the compressor 3.
II est également possible de recycler au moins deux produits et d'envoyer également un gaz 2 riche en un composant du gaz de synthèse provenant d'une source extérieure, autre que l'appareil de séparation, vers l'amont ou l'aval du compresseur de gaz de synthèse. Ce gaz 2 peut être du gaz naturel provenant d'une canalisation ou un gaz de synthèse d'une autre source.  It is also possible to recycle at least two products and also to send a gas 2 rich in a component of the synthesis gas from an external source, other than the separating apparatus, upstream or downstream of the synthesis gas compressor. This gas 2 can be natural gas from a pipe or a synthesis gas from another source.

Claims

Revendications claims
1 . Procédé de séparation d'un gaz de synthèse contenant du monoxyde de carbone et de l'hydrogène dans lequel : 1. Process for the separation of a synthesis gas containing carbon monoxide and hydrogen in which:
i) on comprime un débit de gaz de synthèse (1 ) provenant d'une source de gaz de synthèse dans un compresseur (3)  i) a synthesis gas flow (1) from a source of synthesis gas is compressed in a compressor (3)
ii) on purifie le gaz de synthèse comprimé (15) dans une unité de purification (17) pour l'épurer en eau et/ou en dioxyde de carbone  ii) purifying the compressed synthesis gas (15) in a purification unit (17) to purify it with water and / or carbon dioxide
iii) on refroidit le débit de gaz de synthèse comprimé et purifié  iii) the flow of compressed and purified synthesis gas is cooled
iv) on sépare le débit de gaz de synthèse refroidi par lavage et/ou distillation à une température cryogénique et éventuellement par adsorption dans une unité de séparation (16, 21 , 41 ) et  iv) the cooled synthesis gas flow is separated by washing and / or distillation at a cryogenic temperature and optionally by adsorption in a separation unit (16, 21, 41) and
v) on produit dans l'unité de séparation au moins les trois gaz suivants : un gaz enrichi en monoxyde de carbone (26), un gaz enrichi en hydrogène (43), un gaz résiduaire contenant du monoxyde de carbone et de l'hydrogène (32,47) moins pur en monoxyde de carbone que le gaz enrichi en monoxyde de carbone et moins pur en hydrogène que le gaz enrichi en hydrogène et éventuellement aussi un gaz enrichi en méthane, et/ou un gaz enrichi en azote caractérisé en ce qu'uniquement si le débit de gaz de synthèse envoyé au compresseur est inférieur à un seuil ou nul, on envoie au moins une partie d'au moins deux , voire dechacun des trois gaz suivants :1e gaz enrichi en monoxyde de carbone (26), le gaz enrichi en hydrogène (43) et le gaz résiduaire contenant du monoxyde de carbone et de l'hydrogène (32,47) en aval de la source, et éventuellement en amont du compresseur, pour être purifiés dans l'unité de purification et séparés dans l'unité de séparation.  v) at least one of the following three gases is produced in the separation unit: a carbon monoxide enriched gas (26), a hydrogen enriched gas (43), a carbon monoxide containing waste gas and hydrogen (32,47) less pure in carbon monoxide than the gas enriched in carbon monoxide and less pure in hydrogen than the gas enriched in hydrogen and optionally also a gas enriched in methane, and / or a nitrogen-enriched gas characterized in that only if the synthesis gas flow rate sent to the compressor is below a threshold or zero, is sent at least a portion of at least two, or even each of the following three gases: the carbon monoxide enriched gas (26) , the hydrogen-enriched gas (43) and the residual gas containing carbon monoxide and hydrogen (32,47) downstream of the source, and possibly upstream of the compressor, to be purified in the purification unit and separated in the separation unit.
2. Procédé selon la revendication 1 dans lequel : 2. The method of claim 1 wherein:
a) on stocke du gaz de synthèse comprimé (6) pendant que le débit de gaz de synthèse est supérieur au seuil et  a) compressed synthesis gas (6) is stored while the synthesis gas flow rate is above the threshold and
b) on envoie au moins une partie du gaz de synthèse comprimé ainsi qu'au moins une partie d'au moins chacun des trois premiers gaz de l'étape v) en aval de la source, et éventuellement en amont du compresseur, pour être purifiée dans l'unité de purification et séparés dans l'unité de séparation pendant que le débit de gaz de synthèse est inférieur au seuil. b) at least a portion of the compressed synthesis gas and at least a part of at least each of the first three gases of step v) downstream of the source, and possibly upstream of the compressor, are sent to be purified in the unit of purification and separated in the separation unit while the flow rate of synthesis gas is below the threshold.
3. Procédé selon la revendication 1 ou 2 dans lequel au moins une partie d'au moins chacun des trois gaz (26, 32, 43,47) de l'étape v) en aval de la source et éventuellement en amont du compresseur (3) uniquement si le débit de gaz de synthèse est inférieur au seuil, voire si aucun débit ne provient de la source. 3. The method of claim 1 or 2 wherein at least a portion of at least each of the three gases (26, 32, 43,47) of step v) downstream of the source and possibly upstream of the compressor ( 3) only if the syngas flow is below the threshold, or if no flow is from the source.
4. Procédé selon l'une des revendications précédentes dans lequel on envoie i) x% de la production nominale du gaz enrichi en monoxyde de carbone et y% de la production nominale du gaz enrichi en hydrogène à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, x ety différant d'au plus 5% et/ou 4. Method according to one of the preceding claims wherein i) x% of the nominal production of the carbon monoxide-enriched gas and y% of the nominal production of the hydrogen-enriched gas is sent to the separation unit (16, 21, 41) when the flow rate of synthesis gas is below a threshold, x and y differing by at most 5% and / or
ii°) y% de la production nominale du gaz enrichi en hydrogène et z% de la production nominale du gaz résiduaire à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, y et z différant d'au plus 5% et/ou  (ii) y% of the nominal production of the hydrogen-enriched gas and z% of the nominal production of the waste gas at the separation unit (16, 21, 41) when the synthesis gas flow rate is below one threshold, y and z differing by not more than 5% and / or
ii) x% de la production nominale du gaz enrichi en monoxyde de carbone z% de la production nominale du gaz résiduaire à l'unité de séparation (16, 21 , 41 ) quand le débit de gaz de synthèse est en dessous d'un seuil, x et z différant d'au plus 5%  (ii) x% of the nominal production of the carbon monoxide enriched gas z% of the nominal production of the residual gas at the separation unit (16, 21, 41) when the synthesis gas flow rate is below one threshold, x and z differing by not more than 5%
5. Procédé selon l'une des revendications précédentes dans lequel on stocke une partie (36) du gaz enrichi en monoxyde de carbone dans un stockage (38) et on envoie le reste du gaz enrichi en monoxyde de carbone à un client si le débit de gaz de synthèse est supérieur au seuil et on envoie du gaz enrichi en monoxyde de carbone provenant du stockage au client si le débit de gaz de synthèse est inférieur au seuil. 5. Method according to one of the preceding claims wherein a portion (36) of the carbon monoxide enriched gas is stored in a storage (38) and the remainder of the carbon monoxide enriched gas is sent to a customer if the flow The synthesis gas is above the threshold and carbon monoxide enriched gas from the storage is sent to the customer if the synthesis gas flow rate is below the threshold.
6. Procédé selon la revendication 5 dans lequel si le débit de gaz de synthèse est inférieur au seuil, tout le gaz enrichi en monoxyde de carbone envoyé au client provient du stockage (38) et éventuellement tout le gaz enrichi en monoxyde de carbone provenant directement de l'unité de séparation (16, 21 , 41 ) sans passer pas le stockage (38) est envoyé en amont du compresseur (3) et en aval de la source. 6. The method of claim 5 wherein if the flow rate of synthesis gas is below the threshold, all the carbon monoxide-enriched gas sent to the customer comes from the storage (38) and possibly all the carbon monoxide enriched gas directly from of the separation unit (16, 21, 41) without passing the storage (38) is sent upstream of the compressor (3) and downstream of the source.
7. Procédé selon une des revendications précédentes dans lequel le gaz de synthèse (1 ) est un gaz résiduaire d'une unité de production d'acétylène. 7. Method according to one of the preceding claims wherein the synthesis gas (1) is a waste gas from an acetylene production unit.
8. Procédé selon l'une des revendications précédentes dans lequel si le débit de gaz de synthèse est supérieur au seuil, on stocke une partie du gaz de synthèse dans un stockage (8) et si le débit de gaz de synthèse est inférieur au seuil, on envoie du gaz de synthèse du stockage vers le compresseur (3). 8. Method according to one of the preceding claims wherein if the flow rate of synthesis gas is greater than the threshold, a part of the synthesis gas is stored in a storage (8) and if the flow rate of synthesis gas is below the threshold , synthesis gas is sent from the storage to the compressor (3).
9. Procédé selon l'une des revendications précédentes dans lequel si le débit de gaz de synthèse est nul, l'unité de séparation (16, 21 , 41 ) est alimentée uniquement par des gaz produits par l'unité de séparation. 9. Method according to one of the preceding claims wherein if the flow rate of synthesis gas is zero, the separation unit (16, 21, 41) is fed only by gases produced by the separation unit.
10. Procédé selon l'une des revendications précédentes dans lequel on comprime le gaz enrichi en monoxyde de carbone dans un compresseur de produit (33) et on l'envoie au client et si le débit de gaz de synthèse est inférieur au seuil et le débit de gaz enrichi en monoxyde de carbone à comprimer est inférieur à un autre seuil, on envoie de l'azote gazeux (35) au compresseur de produit pour être comprimé avec le gaz enrichi en monoxyde de carbone. 10. Method according to one of the preceding claims wherein the carbon monoxide enriched gas is compressed in a product compressor (33) and sent to the customer and if the synthesis gas flow rate is below the threshold and the carbon monoxide enriched gas stream to be compressed is below another threshold, nitrogen gas (35) is sent to the product compressor to be compressed with the carbon monoxide enriched gas.
1 1 . Procédé selon l'une des revendications précédentes dans lequel si le débit de gaz de synthèse est inférieur à un seuil, on envoie un gaz riche en un composant du gaz de synthèse (2) provenant d'une autre source qui n'est pas l'unité de séparation à l'unité de séparation(16, 21 , 41 ). 1 1. Process according to one of the preceding claims, in which if the flow rate of synthesis gas is lower than a threshold, a rich gas is sent to a component of the synthesis gas (2) coming from another source which is not the same. separation unit at the separation unit (16, 21, 41).
12. Procédé selon l'une des revendications précédentes dans lequel le gaz enrichi en monoxyde de carbone (26) est comprimé dans un compresseur de produit (33), ensuite divisé en deux, une partie comprimée (39) servant de produit et une partie comprimée (51 ) étant recyclée en aval de la source et/ou le gaz enrichi en hydrogène est comprimé dans un compresseur de produit (22), ensuite divisé en deux, une partie comprimée servant de produit (20) et une partie comprimée (14) étant recyclée en aval de la source (43). 12. A method according to one of the preceding claims wherein the carbon monoxide-enriched gas (26) is compressed in a product compressor (33), then divided into two, a compressed portion (39) serving as a product and a part thereof. compressed (51) being recycled downstream of the source and / or the hydrogen-enriched gas is compressed in a product compressor (22), then divided into two, a compressed product portion (20) and a compressed portion (14). ) being recycled downstream of the source (43).
13. Appareil de séparation d'un gaz de synthèse contenant du monoxyde de carbone et de l'hydrogène comprenant un compresseur (3) pour comprimer un débit de gaz de synthèse (1 ) provenant d'une source de gaz de synthèse, une unité de purification (17) pour épurer en eau et/ou en dioxyde de carbone le gaz de synthèse comprimé (15), des moyens pour refroidir le débit de gaz de synthèse comprimé et purifié, une unité de séparation (16, 21 , 41 ) du débit de gaz de synthèse refroidi par lavage et/ou distillation à une température cryogénique comprenant éventuellement une unité d'adsorption, des moyens pour produire de l'unité de séparation au moins les trois gaz suivants : un gaz enrichi en monoxyde de carbone (26), un gaz enrichi en hydrogène (43), un gaz résiduaire contenant du monoxyde de carbone et de l'hydrogène (32,47) moins pur en monoxyde de carbone que le gaz enrichi en monoxyde de carbone et moins pur en hydrogène que le gaz enrichi en hydrogène et éventuellement aussi un gaz enrichi en méthane, et/ou un gaz enrichi en azote, des moyens pour envoyer au moins une partie d'au moins deux , voire de chacun des trois gaz suivants :1e gaz enrichi en monoxyde de carbone (26), le gaz enrichi en hydrogène (43) et le gaz résiduaire contenant du monoxyde de carbone et de l'hydrogène (32,47) en aval de la source, et éventuellement en amont du compresseur, pour être purifiés dans l'unité de purification et séparés dans l'unité de séparation et des moyens pour déclencher le renvoi d'au moins une partie des au moins deux gaz en fonction du débit de gaz de synthèse provenant de la source en amont du compresseur. 13. Apparatus for separating a synthesis gas containing carbon monoxide and hydrogen comprising a compressor (3) for compressing a flow of synthesis gas (1) from a source of synthesis gas, a unit purification device (17) for purifying the compressed synthesis gas (15) in water and / or carbon dioxide, means for cooling the compressed and purified synthesis gas flow, a separation unit (16, 21, 41) the flow rate of synthesis gas cooled by washing and / or distillation at a cryogenic temperature possibly comprising an adsorption unit, means for producing at least one of the following three gases from the separation unit: a gas enriched in carbon monoxide ( 26), a hydrogen enriched gas (43), a waste gas containing carbon monoxide and hydrogen (32,47) less pure carbon monoxide than the gas enriched in carbon monoxide and less pure hydrogen than the gas enriched in hydrogen and optionally also a gas enriched in methane, and / or a gas enriched in nitrogen, means for sending at least a portion of at least two or even each of the following three gases: the carbon monoxide enriched gas (26), the hydrogen-enriched gas (43) and the residual gas containing carbon monoxide and hydrogen (32,47) downstream of the source, and possibly upstream of the compressor, to be purified in the purification unit and separated in the separation unit and means for triggering the return of at least a portion of the at least two gases as a function of the flow rate of synthesis gas from the source upstream of the compressor.
14. Appareil selon la revendication 13 comprenant un stockage (8) en aval du compresseur (3) et en amont de l'unité de purification (17) ce stockage étant relié à la conduite d'entrée du compresseur par des moyens (10) ne transitant pas par le compresseur. 14. Apparatus according to claim 13 comprising a storage (8) downstream of the compressor (3) and upstream of the purification unit (17) this storage being connected to the inlet pipe of the compressor by means (10) not passing through the compressor.
15. Appareil selon la revendication 14 comprenant des moyens pour envoyer du gaz du stockage en amont du compresseur en fonction du débit de gaz de synthèse provenant de la source en amont du compresseur. 15. Apparatus according to claim 14 comprising means for sending gas from the storage upstream of the compressor as a function of the flow of synthesis gas from the source upstream of the compressor.
EP16809945.5A 2015-10-30 2016-10-28 Method and apparatus for separating a synthesis gas Withdrawn EP3368846A1 (en)

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