FR2969134A1 - Production and treatment of synthesis gas, by generating synthesis gas by gasification, where synthesis gas contains hydrogen, carbon monoxide, carbon dioxide, methane, water and impurities and purifying acidic impurities washing in column - Google Patents

Production and treatment of synthesis gas, by generating synthesis gas by gasification, where synthesis gas contains hydrogen, carbon monoxide, carbon dioxide, methane, water and impurities and purifying acidic impurities washing in column Download PDF

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Publication number
FR2969134A1
FR2969134A1 FR1060888A FR1060888A FR2969134A1 FR 2969134 A1 FR2969134 A1 FR 2969134A1 FR 1060888 A FR1060888 A FR 1060888A FR 1060888 A FR1060888 A FR 1060888A FR 2969134 A1 FR2969134 A1 FR 2969134A1
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France
Prior art keywords
gas
synthesis gas
column
solvent
flash
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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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Application number
FR1060888A
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French (fr)
Inventor
Guylaine Callens-Goregues
Antoine Hernandez
Pascal Marty
Jean-Jacques Talbot
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
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to FR1060888A priority Critical patent/FR2969134A1/en
Publication of FR2969134A1 publication Critical patent/FR2969134A1/en
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • 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
    • C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
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    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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    • 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
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    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
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    • 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
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    • F25J3/0271—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 H2/CO mixtures, i.e. of synthesis gas
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    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
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    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/20—H2/N2 mixture, i.e. synthesis gas for or purge gas from ammonia synthesis
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/02—Separating impurities in general from the feed stream
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract

The process comprises generating synthesis gas by gasification, where the synthesis gas contains hydrogen, carbon monoxide, carbon dioxide (CO 2), methane, water and impurities including sulfur compounds, and purifying all or part of the acidic impurities including CO 2and sulfur compounds by washing in a column using an acid gas solvent, where the purification step comprises prewashing a lower part of a gas column to eliminate impurities of hydrogen sulfide and carbonyl sulfide with a fraction of CO 2solvent and to recovery of the lower part of the column of the solvent to CO 2. The process comprises generating synthesis gas by gasification, where the synthesis gas contains hydrogen, carbon monoxide, carbon dioxide (CO 2), methane, water and impurities including sulfur compounds, and purifying all or part of the acidic impurities including CO 2and sulfur compounds by washing in a column using an acid gas solvent, where the purification step comprises prewashing a lower part of a gas column to eliminate impurities of hydrogen sulfide and carbonyl sulfide with a fraction of CO 2solvent and to recovery of the lower part of the column of the solvent to CO 2and sulfur compounds, washing an upper part of the gas column by an acid gas solvent for absorption of CO 2contained in the gas to be purified and for recovery synthesis gas in the upper part of the column and CO 2solvent in the middle of the column, regenerating the solvent produced by a gas expansion at an average pressure and then regenerating the solvent produced by the gas expansion at low pressure of 3 bar, recycling flash gas in the synthesis gas through single recycle compressor after compression, and cryogenic separating the remaining constituents in the synthesis gas with a production of flash gas of the cold box. The flash gas of the cold box is sent in the compressor for recycling the flash gas and the synthesis gas. The purification step is a step of extraction via a physical solvent of type Rectisol(RTM: Acid gas removal process)/ Selexol(RTM: Acid gas removal solvent) using methanol. The cryogenic separating step is immediately preceded by a purification step. All or part of flash gas from the cold box is used as regeneration gas in the purification step before the flash gas sent to the recycle compressor. An independent claim is included for an installation for production and treatment of synthesis gas.

Description

La présente invention concerne un procédé ainsi qu'une installation pour sa mise en oeuvre, pour la production et le traitement d'un gaz de synthèse dans lequel le procédé comprend au moins les étapes de génération du gaz de synthèse, purification de tout ou partie des impuretés acides parmi lesquelles du dioxyde de carbone et des composés soufrés par lavage dans au moins une colonne de lavage via un solvant de gaz acides, la purification comprenant au moins un prélavage en partie basse de colonne du gaz à purifier pour élimination des impuretés de type H2S et COS, un lavage en partie haute de colonne du gaz issu de la sous-étape par le solvant de gaz acides propre pour absorption du CO2 contenu dans le gaz de synthèse à purifier et récupération en tête de colonne d'un gaz de synthèse purifié et en milieu de colonne de la fraction de solvant chargé en CO2 non utilisée pour le prélavage, une régénération par détente à pression moyenne du solvant issu du prélavage produisant un gaz de détente à moyenne pression, une régénération par détente à pression basse du solvant issu du lavage produisant un gaz de détente à basse pression, un recyclage des gaz de détente après compression dans un compresseur de recycle, ainsi qu'une séparation par voie cryogénique des constituants restant dans le gaz de synthèse avec production de gaz de détente de boîte froide. Le terme gaz de synthèse est de façon courante considéré comme s'appliquant à des mélanges gazeux susceptibles de se combiner pour réaliser la synthèse de composés organiques ou la synthèse d'ammoniac. On trouvera ainsi systématiquement dans les gaz de synthèse les éléments hydrogène, carbone et oxygène, ces deux derniers étant essentiellement combinés entre eux sous forme de monoxyde de carbone (CO) et dioxyde de carbone (CO2); l'hydrogène, essentiellement présent sous forme de gaz hydrogène H 2 forme le constituant essentiel du gaz de synthèse. Les sources principales de gaz de synthèse sont les hydrocarbures (gaz naturel ou coupes pétrolières), mais aussi le charbon, le petcoke et les résidus. Lors de la génération du gaz de synthèse, on opère donc la transformation de C et/ou CnHm en CO, CO2, H2, l'oxygène étant apporté soit directement, soit par de la vapeur d'eau ou de l'air. Cette transformation s'effectue dans un réacteur de reformage à la vapeur (Steam Methane Reformer en anglais ou SMR), ou dans un réacteur d'oxydation d'hydrocarbures, il s'agit alors d'oxydation partielle (PDX), ou de gazéification, ou encore via un reformeur AutoThermique (ATR). On obtient un mélange contenant H2, CO, mais aussi CO2, CH4, H2O, ainsi que S, N2 et des impuretés autres selon la nature de la source et le type de transformation. En aval d'un réacteur de gazéification de charbon, petcoke ou autres résidus, et selon le gaz intermédiaire (H2, CO, mélanges H2 + N2, H2 + CO) à extraire du gaz de synthèse généré (pour la production finale de méthanol, d'acide acétique, d'ammoniac(que) ou de mélanges H2/CO en général), différents schémas de transformation et de purification sont envisagés : - la conversion de CO par la vapeur d'eau en H2 et CO 2 ou réaction de gaz à l'eau (réaction de shift en langue anglaise), - l'extraction de gaz acides par procédé chimique (notamment par lavage aux amines), ou par procédé physique (notamment par lavage au méthanol de type Rectisol/ Selexol), - l'adsorption ou épuration sur lit d'adsorbant, finalisant la purification avant l'entrée du gaz de synthèse (syngas) dans la boîte froide, - la séparation via une boîte froide du syngas pour l'obtention du (des) gaz ou mélanges de gaz ou fluides intermédiaires destinés à la production finale. La boîte froide peut être par exemple : - de type lavage au CO, ou lavage au CH4 ou condensation partielle pour la production intermédiaire conjointe de CO et/ou d'H2 et/ou d'un mélange H2+CO, ou - de type lavage à l'azote pour la production intermédiaire d'un mélange H2+N2). La boîte froide sépare le ou les gaz ou fluides intermédiaires recherchés des autres composés, et génère typiquement un gaz de détente dit « gaz de flash » qui permet par exemple : - d'extraire l'H2 dissous dans la fraction liquide CO issue de la colonne de lavage dans le cas d'une boîte froide de type lavage au CO ou lavage au CH4, - d'extraire l'H2 dissous dans la fraction liquide CO issue du premier pot de condensation dans le cas d'une boîte froide de type condensation partielle, - d'extraire l'H2 dissous dans la fraction liquide d'impuretés (CH4+N2+Ar) issu du premier pot de condensation et/ou de la première colonne de lavage dans le cas d'une boîte froide de type lavage à l'azote. The present invention relates to a method and an installation for its implementation, for the production and treatment of a synthesis gas in which the process comprises at least the synthesis gas generation steps, purification of all or part of acidic impurities including carbon dioxide and sulfur-containing compounds by washing in at least one washing column via an acid gas solvent, the purification comprising at least a prewash at the bottom of the column of the gas to be purified for removal of impurities from type H2S and COS, a washing at the column top of the gas from the sub-step by the clean acid gas solvent for absorption of CO2 contained in the synthesis gas to be purified and recovery at the column head of a gas of purified and column-wise synthesis of the CO2-loaded solvent fraction not used for the prewash, a regeneration by medium pressure expansion of the solvent from the prewash producing a medium pressure flash gas, a low pressure expansion regeneration of the solvent from the wash producing a low pressure flash gas, a recycle of the flash gases after compression in a recycle compressor, and a separation by cryogenic means constituents remaining in the synthesis gas with production of cold box expansion gas. The term synthesis gas is commonly considered to apply to gaseous mixtures capable of combining to effect the synthesis of organic compounds or the synthesis of ammonia. The hydrogen, carbon and oxygen elements are thus systematically found in the synthesis gases, the latter two being essentially combined with each other in the form of carbon monoxide (CO) and carbon dioxide (CO2); hydrogen, essentially present in the form of hydrogen gas H 2 forms the essential constituent of the synthesis gas. The main sources of synthesis gas are hydrocarbons (natural gas or oil cuts), but also coal, petcoke and residues. During the generation of the synthesis gas, the transformation of C and / or CnHm into CO, CO2, H2 is therefore carried out, the oxygen being supplied either directly or by steam or air. This transformation takes place in a steam reforming reactor (Steam Methane Reformer in English or SMR), or in a hydrocarbon oxidation reactor, it is then partial oxidation (PDX), or gasification , or via an AutoThermic reformer (ATR). We obtain a mixture containing H2, CO, but also CO2, CH4, H2O, as well as S, N2 and other impurities according to the nature of the source and the type of transformation. Downstream of a gasification reactor for coal, petcoke or other residues, and according to the intermediate gas (H2, CO, H2 + N2, H2 + CO mixtures) to extract the synthesis gas generated (for the final production of methanol, of acetic acid, ammonia (that) or mixtures H2 / CO in general), different schemes of transformation and purification are envisaged: - the conversion of CO by the water vapor in H2 and CO 2 or reaction of water gas (shift reaction in English language), extraction of acid gases by chemical process (in particular by washing with amines), or by physical process (in particular by washing with Rectisol / Selexol type methanol), the adsorption or purification on an adsorbent bed, finalizing the purification before the entry of the synthesis gas (syngas) into the cold box, - the separation via a cold box of the syngas to obtain the gas (s) or mixtures gas or intermediate fluids for final production. The cold box can be for example: - CO-type wash, or CH4 wash or partial condensation for the joint intermediate production of CO and / or H2 and / or a mixture of H2 + CO, or - of type nitrogen washing for the intermediate production of an H2 + N2 mixture). The cold box separates the gas or desired intermediate fluids from the other compounds, and typically generates a flash gas called "flash gas" which allows for example: - to extract the dissolved H2 in the liquid fraction CO from the washing column in the case of a cold box of the CO washing or CH4 washing type, extracting the H2 dissolved in the CO liquid fraction from the first condensation pot in the case of a cold box of the type partial condensation, - to extract the H2 dissolved in the liquid impurity fraction (CH4 + N2 + Ar) from the first condensation pot and / or the first washing column in the case of a cold box of the type nitrogen wash.

Dans tous les cas, le « gaz de flash » contient une proportion majoritaire d'H2 et de CO, et une proportion minoritaire de CH4, N2, et d'Argon. Ce gaz de flash peut être par la suite valorisé, soit : - en étant dirigé dans un réseau fuel pour alimenter une combustion et satisfaire ainsi des besoins thermiques, - en étant dirigé en entrée de l'unité d'extraction des gaz acides ou de la boîte froide via un compresseur dédié. Il ressort de l'ensemble des étapes de procédé décrites ci-dessus que le CO2 est un composé présent dans un gaz de synthèse, à la fois en tant que produit obtenu lors d'un reformage ou d'une oxydation partielle, et naturellement comme produit résultant de la conversion du monoxyde de carbone (shift). Or, si le CO2 est accepté et même utilisé dans la synthèse du méthanol, il est par contre un constituant inutile et même nuisible du gaz de synthèse destiné à d'autres productions (synthèse d'ammoniac(que) par exemple). Il en est de même pour les procédés de production d'hydrogène. Il est donc fréquemment nécessaire d'éliminer le CO2 lors du traitement du syngas (en aval de l'étape de conversion de CO quand celle-ci existe). Ainsi que rapporté ci-dessus, le CO2 (gaz acide) peut être extrait par lavage avec différents absorbants, parmi lesquels les amines et les solvants, en particulier le méthanol. Par ailleurs, lorsque le gaz de synthèse est obtenu par oxydation partielle d'hydrocarbures, en particulier par gazéification de charbon, de petcoke ou de résidus, on trouve aussi des composés de soufre (H2S, ...) présents dans le gaz de synthèse qui doivent donc être éliminés au même titre que le CO2. Dans ce cas, on emploie généralement des procédés mixtes qui utilisent des solutions absorbant les composés soufrés et le CO2, et on préfère tout particulièrement les procédés permettant d'absorber ces composés sélectivement. C'est ainsi que parmi ces procédés mixtes et sélectifs, les procédés dits physiques sont particulièrement intéressants, notamment les procédés de type Rectisol/ Selexol. Utilisant le méthanol comme solvant des gaz acides, le procédé Rectisol utilise ainsi les caractéristiques suivantes des produits : les gaz acides H2S et CO2 sont très solubles dans le méthanol, l'affinité du solvant pour H2S étant cependant beaucoup plus importante que pour CO2. Il est alors possible d'éliminer sélectivement ces composés. Ainsi, dans le cadre d'un procédé d'élimination des gaz acides contenus dans un gaz de synthèse brut obtenu par oxydation partielle suivie d'une réaction de shift (conversion de CO et H2O en H2 et CO2), on obtient un gaz de grande pureté. Le procédé comporte pour cela typiquement les étapes suivantes : - Le gaz de synthèse est refroidi à contre courant des flux de produits froids issus du procédé d'élimination des gaz acides, du méthanol étant injecté dans le gaz de synthèse afin de prévenir la formation de glace ; - Les étapes suivantes d'extraction des gaz acides sont réalisées dans la colonne dite de lavage, le gaz de synthèse étant introduit en partie basse de la colonne : - dans une première étape dite de prélavage, en section basse de la colonne de lavage, les composés H2S et COS sont « lavés » avec une fraction du solvant chargé en CO2 provenant de la section supérieure de lavage du CO2, cette fraction du solvant est aussi dite « méthanol pre-wash » ; - le CO2 contenu dans le gaz de synthèse est ensuite absorbé par lavage avec du méthanol propre injecté en tête de la colonne de lavage. Le gaz de synthèse débarrassé des gaz acides est alors récupéré en tête de colonne ; - le méthanol chargé en CO2 et en composés soufrés, récupéré en fond de la section basse de la colonne de lavage est régénéré par un système de détentes successives à moyenne pression (8 à 10 bar), produisant ainsi un gaz de flash ; - le méthanol chargé en CO2 (provenant de la section supérieure - moins la fraction de « methanol pre-wash ») est régénéré par un système de détentes successives à basse pression (aux alentours de 3 bar), produisant ainsi un second gaz de flash. Lors des étapes décrites ci-dessus de lavage du gaz de synthèse, des produits valorisables sont entraînés, (H2, CO, CO2), ce qui rend tout à fait intéressant leur recyclage dans le gaz de synthèse à l'entrée de l'unité d'extraction de gaz acides. Cependant, disponibles à des pressions très inférieures à la pression d'alimentation en gaz de synthèse de la colonne de lavage au méthanol, une compression est nécessaire. In all cases, the "flash gas" contains a majority proportion of H2 and CO, and a minor proportion of CH4, N2, and argon. This flash gas can then be upgraded, either: - by being directed into a fuel network to supply combustion and thus meet thermal needs, - by being directed at the inlet of the acid gas extraction unit or the cold box via a dedicated compressor. It emerges from all the process steps described above that CO2 is a compound present in a synthesis gas, both as a product obtained during a reforming or a partial oxidation, and naturally as product resulting from the conversion of carbon monoxide (shift). However, if the CO2 is accepted and even used in the synthesis of methanol, it is against a useless and even harmful constituent of the synthesis gas for other productions (ammonia synthesis (for example)). It is the same for hydrogen production processes. It is therefore frequently necessary to eliminate CO2 during the treatment of syngas (downstream of the CO conversion step when this exists). As mentioned above, the CO2 (acid gas) can be extracted by washing with various absorbents, among which amines and solvents, in particular methanol. Moreover, when the synthesis gas is obtained by partial oxidation of hydrocarbons, in particular by gasification of coal, petcoke or residues, there are also sulfur compounds (H2S, ...) present in the synthesis gas. which must be eliminated in the same way as CO2. In this case, mixed processes are generally employed which utilize solutions that absorb sulfur compounds and CO2, and methods for selectively absorbing these compounds are most preferred. Thus, among these mixed and selective processes, the so-called physical processes are particularly interesting, especially the Rectisol / Selexol type processes. Using methanol as a solvent for acid gases, the Rectisol process thus uses the following characteristics of the products: the acid gases H2S and CO2 are very soluble in methanol, although the affinity of the solvent for H2S is much greater than for CO2. It is then possible to selectively remove these compounds. Thus, in the context of a process for removing acid gases contained in a crude synthesis gas obtained by partial oxidation followed by a shift reaction (conversion of CO and H2O to H2 and CO2), a gas is obtained. high purity. For this purpose, the process typically comprises the following steps: the synthesis gas is countercurrently cooled with cold product streams resulting from the acid gas removal process, methanol being injected into the synthesis gas in order to prevent the formation of ice cream ; The following stages of extraction of the acid gases are carried out in the so-called washing column, the synthesis gas being introduced at the bottom of the column: in a first so-called prewashing step, in the lower section of the washing column, the H2S and COS compounds are "washed" with a fraction of the solvent loaded with CO2 coming from the upper section for washing CO2, this fraction of the solvent is also called "methanol pre-wash"; the CO2 contained in the synthesis gas is then absorbed by washing with clean methanol injected at the top of the washing column. The synthesis gas freed from acid gases is then recovered at the top of the column; - The methanol loaded with CO2 and sulfur compounds, recovered at the bottom of the lower section of the washing column is regenerated by a system of successive expansion at medium pressure (8 to 10 bar), thereby producing a flash gas; the methanol charged with CO2 (from the upper section - minus the fraction of "methanol pre-wash") is regenerated by a system of successive low-pressure detents (at around 3 bar), thus producing a second flash gas . During the steps described above for washing the synthesis gas, recoverable products are entrained, (H2, CO, CO2), which makes it quite interesting to recycle them in the synthesis gas at the inlet of the unit. acid gas extraction. However, available at pressures much lower than the synthesis gas feed pressure of the methanol wash column, compression is required.

Les gaz de flash issus de ces étapes de régénération par détente à moyenne et basse pression sont comprimés - en général via un compresseur unique de recycle - et renvoyés dans le gaz de synthèse alimentant la colonne de lavage de sorte à valoriser les produits contenus (H2, CO, CO2). The flash gases resulting from these regeneration steps by medium and low pressure expansion are compressed - generally via a single recycle compressor - and returned to the synthesis gas supplying the washing column so as to enhance the products contained (H2 , CO, CO2).

Les détentes à moyenne et basse pression permettant ainsi de désorber les gaz acides contenus dans les deux fractions du solvant usé constituent la première régénération, après cette première régénération, on poursuit par une régénération chaude du méthanol réalisée par stripage par un gaz inerte (N2), par l'air ou par de la vapeur d'eau, de sorte à récupérer du méthanol propre et apte à être réinjecté en tête de la colonne de lavage, ainsi que des produits (S et CO2), disponibles pour des utilisations ultérieures. Ainsi, les étapes de purification/séparation décrites ci-dessus qui constituent des étapes essentielles dans le traitement du gaz de synthèse génèrent différents courants gazeux résiduaires qui sont à l'heure actuelle couramment valorisés, mais dont l'utilisation n'est pas toujours optimisée. C'est pourquoi, selon un objet de l'invention, il est proposé un procédé de production et de traitement d'un gaz de synthèse, ledit procédé comprenant au moins les étapes suivantes : a) génération d'un gaz de synthèse, contenant principalement de l'hydrogène, du monoxyde de carbone, mais aussi du dioxyde de carbone, du méthane, de l'eau, ainsi que des impuretés, dont potentiellement des composés soufrés ; b) purification de tout ou partie des impuretés acides parmi lesquelles du dioxyde de carbone et des composés soufrés par lavage dans au moins une colonne de lavage via un solvant de gaz acides, comprenant au moins les étapes suivantes : b-1) prélavage en partie basse de colonne du gaz à purifier pour élimination des impuretés de type H2S, COS avec une fraction du solvant chargé en CO2 produit par l'étape b-2), avec récupération en bas de colonne du solvant chargé en CO2 et en composés soufrés, b-2) lavage en partie haute de colonne du gaz issu de l'étape b-1) par ledit solvant de gaz acides propre pour absorption du CO2 contenu dans ledit gaz à purifier et récupération en tête de colonne d'un gaz de synthèse purifié et en milieu de colonne de la fraction de solvant chargé en 002 non utilisée dans l'étape b-1), b-3) régénération par détente à pression moyenne du solvant issu de la sous étape 1) produisant un gaz de détente à pression moyenne, b-4) régénération par détente à pression basse (de l'ordre de 3 bar) du solvant issu de la sous étape 2) produisant un gaz de détente à basse pression ; c) recyclage, après compression - de préférence via un compresseur unique de recycle - des gaz de détente issus des étapes b-3 et b-4) dans le gaz de synthèse à purifier alimentant l'étape de purification b) ; d) séparation par voie cryogénique des constituants restant dans le gaz de synthèse issu de l'étape b-2) avec production d'un gaz de détente dit de boîte froide ; caractérisé en ce que le gaz de détente de boîte froide issu de l'étape d) est envoyé, partiellement ou totalement, dans le compresseur de l'étape c) pour être recyclé avec les gaz de détente issus des étapes b-3) et b-4) dans le gaz de synthèse à purifier alimentant l'étape de purification b). Le procédé de l'invention est de préférence un procédé dans lequel l'étape a) de génération de gaz de synthèse est une étape de gazéification. The medium and low pressure detents thus making it possible to desorb the acid gases contained in the two fractions of the spent solvent constitute the first regeneration, after this first regeneration, a warm regeneration of the methanol carried out by stripping with an inert gas (N2) is continued. , by air or by steam, so as to recover clean methanol and suitable to be reinjected at the top of the washing column, as well as products (S and CO2), available for subsequent uses. Thus, the purification / separation steps described above which constitute essential steps in the treatment of synthesis gas generate different gaseous waste streams which are at present commonly valued, but whose use is not always optimized. . Therefore, according to one object of the invention, there is provided a method for producing and treating a synthesis gas, said method comprising at least the following steps: a) generation of a synthesis gas, containing mainly hydrogen, carbon monoxide, but also carbon dioxide, methane, water, as well as impurities, including potentially sulfur compounds; b) purification of all or part of the acidic impurities including carbon dioxide and sulfur-containing compounds by washing in at least one washing column via an acid gas solvent, comprising at least the following steps: b-1) partial prewash column bottom of the gas to be purified for removal of the H2S, COS type impurities with a fraction of the CO2-loaded solvent produced by step b-2), with recovery at the bottom of the column of the solvent loaded with CO2 and sulfur compounds, b-2) washing at the top of the column of the gas resulting from step b-1) by said clean acid gas solvent for absorbing the CO2 contained in said gas to be purified and recovery at the column head of a synthesis gas purified and in the middle of the column of the fraction of solvent loaded in 002 not used in step b-1), b-3) regeneration by expansion at medium pressure of the solvent from sub-step 1) producing a flash gas at average pressure, b-4) reg eration by low pressure expansion (of the order of 3 bar) of the solvent from the sub-step 2) producing a low pressure flash gas; c) recycling, after compression - preferably via a single recycle compressor - expansion gases from steps b-3 and b-4) in the synthesis gas to be purified, feeding the purification step b); d) cryogenic separation of the constituents remaining in the synthesis gas from step b-2) with production of a so-called cold box expansion gas; characterized in that the cold box expansion gas from step d) is sent, partially or totally, into the compressor of step c) to be recycled with the flash gases from steps b-3) and b-4) in the synthesis gas to be purified, supplying the purification step b). The process of the invention is preferably a process in which step a) of generating synthesis gas is a gasification step.

De préférence, l'étape d'extraction est une étape d'extraction via un solvant physique, de type Rectisol/Selexol utilisant du méthanol en tant que solvant physique. L'étape d) de séparation cryogénique pouvant être immédiatement précédée par une étape de purification en tête par adsorption, tout ou partie du gaz de détente de la boîte froide pourra être utilisé comme gaz de régénération dans ladite étape de purification en tête avant d'être envoyé au compresseur de recycle avec les gaz de détente de l'étape 2). Selon un autre objet de l'invention, il est prévu une installation pour la production et le traitement d'un gaz de synthèse, ladite installation comprenant au moins une unité de génération de gaz de synthèse par gazéification d'une charge de type charbon, petcoke, résidus, une unité d'extraction de gaz acides par lavage au méthanol, de type Rectisol ou Selexol, munie d'un compresseur de recycle des gaz de détente, une unité d'épuration en tête, une boîte froide, des moyens de conduit reliant les différents moyens ci-dessus, ainsi que des moyens de conduit pour envoyer une proportion non nulle du gaz de détente de la boîte froide vers le compresseur de recycle des gaz de détente de l'unité d'extraction, et des moyens de conduit pour recycler les gaz de détente comprimés dans le gaz de synthèse alimentant ladite unité d'extraction. L'installation peut être adaptée pour mettre en oeuvre un quelconque des procédés tels que définis précédemment. Preferably, the extraction step is a physical solvent extraction step of the Rectisol / Selexol type using methanol as the physical solvent. Since the cryogenic separation stage d) can be immediately preceded by an adsorption head purification stage, all or part of the expansion gas of the cold box can be used as a regeneration gas in the said head purification step before be sent to the recycle compressor with the flash gases of step 2). According to another object of the invention, there is provided an installation for the production and treatment of a synthesis gas, said installation comprising at least one unit for generating synthesis gas by gasification of a coal-type charge, petcoke, residues, a unit of extraction of acid gas by washing with methanol, of the Rectisol or Selexol type, equipped with a recycle gas compressor, a purification unit at the head, a cold box, means of conduit connecting the various means above, as well as conduit means for sending a non-zero proportion of the flash gas from the cold box to the compressor recycle gas expansion of the extraction unit, and means of conducted to recycle compressed flash gases into the synthesis gas supplying said extraction unit. The installation can be adapted to implement any of the methods as defined above.

Les avantages du procédé selon l'invention résultent de l'utilisation optimisée du compresseur de recycle des gaz de flash de l'unité d'extraction de gaz acides, et de l'utilisation optimisée du gaz de flash de la boîte froide. Il s'agit en particulier : - d'une amélioration des rendements de production de CO et/ou d'H2 (et/ou de mélanges), - d'une diminution de la quantité de CO2 émise à l'atmosphère (moins de CO et d'H2 brûlés au fuel) par rapport à la solution où le « gaz de flash » serait envoyé vers un réseau fuel, ainsi que - d'un gain d'investissement par rapport à la solution qui consisterait à recycler séparément le gaz de flash de la boîte froide et les gaz riches en produits valorisables. The advantages of the process according to the invention result from the optimized use of the flash gas recycle compressor of the acid gas extraction unit, and the optimized use of flash gas from the cold box. This concerns in particular: - an improvement in the production yields of CO and / or H2 (and / or mixtures), - a decrease in the amount of CO2 emitted to the atmosphere (less than CO and H2 burned in fuel) compared to the solution where the "flash gas" would be sent to a fuel network, as well as - an investment gain compared to the solution that would be to recycle the gas separately cold box flash and gas rich in valuable products.

Claims (6)

REVENDICATIONS1. Procédé de production et de traitement d'un gaz de synthèse, ledit procédé comprenant au moins les étapes suivantes : a) génération d'un gaz de synthèse, contenant principalement de l'hydrogène, du monoxyde de carbone, mais aussi du dioxyde de carbone, du méthane, de l'eau, ainsi que des impuretés, dont potentiellement des composés soufrés ; b) purification de tout ou partie des impuretés acides parmi lesquelles du dioxyde de carbone et des composés soufrés par lavage dans au moins une colonne de lavage via un solvant de gaz acides, comprenant au moins les étapes suivantes : b-1) prélavage en partie basse de colonne du gaz à purifier pour élimination des impuretés de type H2S, COS avec une fraction du solvant chargé en CO2 produit par l'étape b-2), avec récupération en bas de colonne du solvant chargé en CO2 et en composés soufrés, b-2) lavage en partie haute de colonne du gaz issu de l'étape b-1) par ledit solvant de gaz acides propre pour absorption du CO2 contenu dans ledit gaz à purifier et récupération en tête de colonne d'un gaz de synthèse purifié et en milieu de colonne de la fraction de solvant chargé en CO2 non utilisée dans l'étape b-1), b-3) régénération par détente à pression moyenne du solvant issu de l'étape b-1) produisant un gaz de détente à pression moyenne, b-4) régénération par détente à pression basse (de l'ordre de 3 bar) du solvant issu de l'étape b-2) produisant un gaz de détente à basse pression ; 20 25 30 c) recyclage, après compression - de préférence via un compresseur unique de recycle - des gaz de détente issus des sous étapes b-1) et b-2) dans le gaz de synthèse à purifier alimentant l'étape de purification b) ; d) séparation par voie cryogénique des constituants restant dans le gaz de synthèse issu de l'étape b) avec production d'un gaz de détente dit de boîte froide ; caractérisé en ce que le gaz de détente de boîte froide issu de l'étape d) est envoyé, partiellement ou totalement, dans le compresseur de l'étape c) pour être recyclé avec les gaz de détente issus des étapes b-3) et b-4) dans le gaz de synthèse à purifier alimentant l'étape de purification b). REVENDICATIONS1. A method for producing and processing a synthesis gas, said method comprising at least the following steps: a) generating a synthesis gas, mainly containing hydrogen, carbon monoxide, but also carbon dioxide methane, water, and impurities, including potentially sulfur compounds; b) purification of all or part of the acidic impurities including carbon dioxide and sulfur-containing compounds by washing in at least one washing column via an acid gas solvent, comprising at least the following steps: b-1) partial prewash column bottom of the gas to be purified for removal of the H2S, COS type impurities with a fraction of the CO2-loaded solvent produced by step b-2), with recovery at the bottom of the column of the solvent loaded with CO2 and sulfur compounds, b-2) washing at the top of the column of the gas resulting from step b-1) by said clean acid gas solvent for absorbing the CO2 contained in said gas to be purified and recovery at the column head of a synthesis gas purified and in the middle of the column of the fraction of solvent loaded with CO2 not used in step b-1), b-3) regeneration by expansion at medium pressure of the solvent resulting from step b-1) producing a gas of relaxation at medium pressure, b-4) regenerated low pressure expansion (of the order of 3 bar) of the solvent from step b-2) producing a low pressure flash gas; C) recycling, after compression - preferably via a single recycle compressor - expansion gases from substeps b-1) and b-2) in the synthesis gas to be purified feeding the purification step b ); d) cryogenic separation of the constituents remaining in the synthesis gas from step b) with production of a so-called cold box expansion gas; characterized in that the cold box expansion gas from step d) is sent, partially or totally, into the compressor of step c) to be recycled with the flash gases from steps b-3) and b-4) in the synthesis gas to be purified, supplying the purification step b). 2. Procédé selon la revendication 1, dans lequel l'étape a) de génération de gaz de synthèse est une étape de gazéification. The process of claim 1, wherein the synthesis gas generating step a) is a gasification step. 3. Procédé selon une des revendications 1 ou 2 dans lequel l'étape d'extraction est une étape d'extraction via un solvant physique, de type Rectisol/Selexol utilisant du méthanol en tant que solvant physique. 3. Method according to one of claims 1 or 2 wherein the extraction step is an extraction step via a physical solvent, Rectisol / Selexol type using methanol as a physical solvent. 4. Procédé selon l'une des revendications 1 à 3, dans lequel l'étape d) de séparation cryogénique est immédiatement précédée par une étape de purification en tête par adsorption, et dans lequel tout ou partie du gaz de détente de la boîte froide est utilisé comme gaz de régénération dans ladite étape de purification en tête avant d'être envoyé au compresseur de recycle avec les gaz de détente de l'étape ). 4. Method according to one of claims 1 to 3, wherein the cryogenic separation step d) is immediately preceded by a step of head purification by adsorption, and wherein all or part of the expansion gas of the cold box. is used as a regeneration gas in said overhead purification step before being sent to the recycle compressor with the flash gases of the step). 5. Installation pour la production et le traitement d'un gaz de synthèse, ladite installation comprenant au moins: - une unité de génération de gaz de synthèse par gazéification d'une charge de type charbon, petcoke, résidus, 2- une unité d'extraction de gaz acides par lavage au méthanol, de type Rectisol ou Selexol, munie d'un compresseur de recycle des gaz de détente, - une unité d'épuration en tête, - une boîte froide, - des moyens de conduit reliant les différents moyens, caractérisée en ce qu'elle comprend des moyens de conduit pour envoyer une proportion non nulle du gaz de détente de la boîte froide vers le compresseur de recycle des gaz de détente de l'unité d'extraction, et des moyens de conduit pour recycler les gaz de détente comprimés dans le gaz de synthèse alimentant ladite unité d'extraction. 5. Installation for the production and treatment of a synthesis gas, said installation comprising at least: a unit for generating synthesis gas by gasification of a charge of the coal, petcoke, residues type, a unit of extraction of acidic gases by washing with methanol, of the Rectisol or Selexol type, equipped with a recycle compressor for the expansion gases, - a purification unit at the head, - a cold box, - conduit means connecting the different means, characterized in that it comprises conduit means for sending a non-zero proportion of the flash gas from the cold box to the recycle compressor of the flash gases of the extraction unit, and conduit means for recycling the compressed flash gases into the synthesis gas supplying said extraction unit. 6. Installation selon la revendication précédente dans laquelle l'installation est adaptée ou construite pour mettre en oeuvre le procédé tel que défini à l'une quelconque des revendications 2 à 4. 20 6. Installation according to the preceding claim wherein the installation is adapted or constructed to implement the method as defined in any one of claims 2 to 4. 20
FR1060888A 2010-12-21 2010-12-21 Production and treatment of synthesis gas, by generating synthesis gas by gasification, where synthesis gas contains hydrogen, carbon monoxide, carbon dioxide, methane, water and impurities and purifying acidic impurities washing in column Withdrawn FR2969134A1 (en)

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