WO2012175635A2 - Procédé et installation de production d'oxyde carbonique gazeux par distillation cryogénique - Google Patents

Procédé et installation de production d'oxyde carbonique gazeux par distillation cryogénique Download PDF

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Publication number
WO2012175635A2
WO2012175635A2 PCT/EP2012/062020 EP2012062020W WO2012175635A2 WO 2012175635 A2 WO2012175635 A2 WO 2012175635A2 EP 2012062020 W EP2012062020 W EP 2012062020W WO 2012175635 A2 WO2012175635 A2 WO 2012175635A2
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WO
WIPO (PCT)
Prior art keywords
carbon monoxide
liquefied
conduit
product
separation unit
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PCT/EP2012/062020
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English (en)
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WO2012175635A3 (fr
Inventor
Emmanuelle BROCHERIOU
Bhadri PRASAD
Audrey RIVOAL
Marie-Pascal Victor
Original Assignee
L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
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Application filed by L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude filed Critical L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
Priority to CN201280030991.7A priority Critical patent/CN104011488B/zh
Publication of WO2012175635A2 publication Critical patent/WO2012175635A2/fr
Publication of WO2012175635A3 publication Critical patent/WO2012175635A3/fr

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Classifications

    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—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 CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0261—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon monoxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/08—Internal refrigeration by flash gas recovery loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/24—Quasi-closed internal or closed external carbon monoxide refrigeration cycle
    • 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
    • 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/20—Control for stopping, deriming or defrosting after an emergency shut-down of the installation or for back up system

Definitions

  • This invention concerns processes and installations for providing gaseous carbon monoxide by cryogenic distillation.
  • it concerns the supply of carbon monoxide by vaporisation of liquid carbon monoxide when an industrial installation, such as a separation unit, requires a rapidly increasing amount of gaseous carbon monoxide product.
  • EP-A-1479989 suggests that the liquid can be stored at high pressure or pumped so as to produce carbon monoxide directly at the product pressure. However this involves the cost of a pump or of a high pressure storage, which also carries a security risk.
  • the CO liquid from the cycle is removed before expansion into the top reboiler of a column and is vaporized at the desired pressure (for example, that of the client's network).
  • the amount of gaseous carbon monoxide produced can increase by at least 1 % per minute.
  • a feed gas containing carbon monoxide as at least one of its principal components and at least one other components chosen from methane, nitrogen and hydrogen, is purified using an adsorption step in one of at least two adsorbent beds to produce a purified feed gas to be sent to the separation unit comprising at least one distillation column,
  • the separation unit separates the feed gas to produce gaseous carbon monoxide and the gaseous carbon monoxide is compressed in a product compressor to produce a final product at a product pressure
  • a carbon monoxide cooling cycle in which a cycle fluid is compressed in at least the product compressor, cooled and expanded wherein at least part of the carbon monoxide is used to reboil a distillation column of the separation unit at the highest pressure of the cycle and is liquefied to form pressurised liquefied carbon monoxide, a first part of the liquefied carbon monoxide being expanded from the highest pressure to a lower pressure and sent to a top condenser of a distillation column of the separation unit, and
  • a second part of the pressurised liquefied carbon monoxide is expanded from the highest pressure to the product pressure and is vaporised at the product pressure without having been stored in any storage vessel and upstream of the top condenser to form a pressurised gaseous back-up stream which is then mixed with the final product, vaporisation of the carbon monoxide taking place only when there is an increase in demand for pressurised carbon monoxide.
  • the separation unit comprises a cryogenic CO/CH distillation column, having a top condenser and/or CO liquid storage capacity and wherein the liquefied carbon monoxide is expanded and sent to the top condenser in normal operation and, if there is an increase in demand for pressurised carbon monoxide, the liquefied carbon monoxide is vaporised without having been sent to the top condenser.
  • the liquefied carbon monoxide is vaporised at a pressure higher than the lower pressure of step c).
  • the liquefied carbon monoxide is liquefied by reboiling at least one column of the separation unit.
  • an installation for supplying gaseous carbon monoxide by cryogenic distillation including:
  • a separation unit including at least one distillation column.
  • a carbon monoxide refrigeration cycle for cooling the installation, the cycle including conduits for sending refrigeration cycle carbon monoxide to the product compressor, means for liquefying the refrigeration cycle carbon monoxide by sending the carbon monoxide cycle fluid to at least one distillation column reboiler of the separation unit at the highest pressure of the cycle, the cycle comprising no storage vessel for cycle fluid other than a top condenser of a distillation column.
  • a conduit for sending a first part of liquefied refrigeration cycle carbon monoxide to the top condenser said conduit being connected to expansion means for expanding the first part upstream of the top condenser.
  • a conduit for sending a second part of liquefied refrigeration cycle carbon monoxide to the vaporiser the conduit being connected downstream of at least one distillation column reboiler without any intervening storage vessel and to an expansion valve for expanding the second part from the highest pressure of the cycle to the product pressure.
  • a back-up conduit for removing vaporised refrigeration cycle carbon monoxide from the vaporiser, the back-up conduit being connected to the product carbon monoxide conduit, there being no compressor between the vaporiser and the point where the back-up conduit connects to the product carbon monoxide conduit.
  • Optional features include:
  • the separation unit comprises a cryogenic CO/CH distillation column , having a top condenser and/or CO liquid storage capacity , means for expanding liquefied carbon monoxide and means for sending the expanded liquefied carbon monoxide to the top condenser and/or CO liquid capacity.
  • the separation unit comprises a nitrogen wash column.
  • the separation unit comprises a methane wash column.
  • the refrigeration cycle includes means for sending the refrigeration cycle carbon monoxide to a reboiler of at least one column of the separation unit, for example the CO/CH column, and means for sending the refrigeration cycle carbon monoxide liquefied in the reboiler at least to the vaporiser.
  • the installation comprises a heat exchanger for cooling the liquefied carbon monoxide by heat exchange with gaseous carbon monoxide and a conduit for sending the warmed carbon monoxide to the product compressor.
  • the conduit for sending a second part of liquefied refrigeration cycle carbon monoxide to the vaporiser removes the second part at a point upstream of the top condenser.
  • the installation comprises an exchanger for cooling the liquefied refrigeration cycle carbon monoxide downstream of the column reboiler(s).
  • the installation comprises a conduit for sending liquefied refrigeration cycle carbon monoxide to the vaporiser without passing through a column reboiler.
  • Figure 1 shows an apparatus for separating a mixture containing principally methane, carbon monoxide and hydrogen.
  • the mixture may also contain small amounts of nitrogen, carbon dioxide, humidity, higher hydrocarbons, methanol, etc.
  • This mixture is generally synthesis gas produced by a partial oxidation unit, a steam methane reformer, an auto thermal reformer, gasifier or any combination of these process schemes.
  • the mixture 1 is purified in a front end purification unit to remove impurities. Then the mixture is cooled to a cryogenic temperature in heat exchangers 3, 5 and sent to the bottom of a methane wash column 7 operating at a pressure between 10 and 60 bars. A methane wash stream 9 is fed to the top of column 7 and a hydrogen enriched stream 1 1 is removed from the top of the column. From the bottom of the column is removed a liquid stream 13 enriched in carbon monoxide.
  • Stream 13 is further treated before being sent to the stripping column 19 which operates at between 4 and 17 bars, at least one feed stream formed from stream 13 being sent to the top of stripping column 19. Alternatively if a methane stream is fed to the top of stripping column 19, the feed stream is fed thereto at a lower point.
  • the gas 21 from the top of the stripping column is warmed in the exchangers 5, 3 and is used as fuel or burnt.
  • the liquid stream 23 from the bottom of the stripping column 19 is divided in two and may be further treated before being sent to the column 27. In particular, several feeds (liquid, dual phase, gaseous, in this case two liquid streams) at different levels may be provided to the column 27. Column 27 operates at between 1 and 10 bars, often around 2.5 bars.
  • methane rich liquid 29 at the bottom of the column and a carbon monoxide rich gas 31 at the top of the column.
  • Part of the methane rich liquid is pumped by pump 33 and sent to the top of the methane wash column 7 and the rest is removed as a purge stream.
  • the two portions of the methane rich liquid may be removed separately from the column.
  • the methane rich liquid is pumped by pump 33 and sent in part to the top of the methane wash column 7 and the remaining purge stream is warmed in heat exchangers 5, 3.
  • the carbon monoxide rich product stream 31 removed from the top of column 27 is warmed in a heat exchanger 52 and then in heat exchanger 3, compressed in a compressor 35 and is removed as a compressed product gas 37.
  • Refrigeration for the system is provided by a carbon monoxide cycle of which the compressor 35 forms part.
  • the carbon monoxide is compressed in compressor 35 to a pressure of between 10 and 60 bars.
  • Part of the compressed carbon monoxide 39 is further compressed in compressor 35A, then cooled in exchanger 3 to an intermediate temperature of the exchanger and then expanded in turbine 41 .
  • the expanded carbon monoxide gas is warmed in the exchanger 3 and recycled to the compressor 35 at the entry thereof or an intermediate pressure thereof.
  • the unexpanded carbon monoxide 43 is divided into three parts, two of which, namely parts 51 , 53, serve to reboil columns 9 and 1 1 .
  • Part 51 is sent to reboiler 55 of column 19 and part 53 is sent to the reboiler 57 of column 27.
  • the cooled parts are then both further cooled in heat exchanger 52 from which they are removed as liquid streams.
  • Stream 53 is entirely sent to top condenser and/or CO liquid storage capacity 47 of column 27 via open expansion valve V3.
  • all of stream 51 is also sent to top condenser and/or CO liquid storage capacity 47 via open expansion valve V2, valve V1 being closed.
  • the top condenser and/or CO storage liquid capacity 47 forms an integral part of the column 27 and additionally serves to provide reflux to the top of column 27 and to supply liquid carbon monoxide to cool an intermediate reboiler 49 of the methane wash column 7.
  • a further part 59 of the unexpanded carbon monoxide 43 is cooled in exchangers 3, 5 and sent to the top condenser or storage 47 via expansion valve V5.
  • part 59A of the carbon monoxide is sent via open valve V6, which is not an expansion valve, to vaporiser 54, replacing at least one of streams 51 , 53 or in addition to at least one of these streams.
  • part 51 A or all of the liquid 51 may be vaporised in a vaporiser 54 upstream of the top condenser and/or CO liquid capacity 47 by opening expansion valve V1 to expand the gas from the outlet pressure of compressor 35A to the outlet pressure of compressor 35 and at least partially closing valve V2.
  • the carbon monoxide stream sent to vaporiser 54 is produced substantially at the outlet pressure of compressor 35.
  • the vaporiser 54 may either allow heat exchange with ambient air, water or steam if it is outside the cold box or may be within the cold box and may be constituted by the exchanger 5 or another heat exchanger.
  • the vaporised carbon monoxide produced 55 is sent to a point downstream of the compressor 35 to form part of the product gas 37.
  • the liquid to be vaporised 51 , 53 is available at high pressure, i.e. a pressure higher than that of condenser (or storage) 47, the gas produced, by vaporisation in vaporiser 54, can be directly mixed with the product gas 37 after expansion in at least one of valves V1 ,V4.
  • Gaseous and liquid carbon monoxide are defined to be respectively a gas and a liquid containing at least 85% carbon monoxide, preferably at least 95% carbon monoxide.
  • cryogenic separation processes for mixtures containing carbon monoxide and at least one of hydrogen, nitrogen and methane as principal components, for example processes to separate mixtures of hydrogen, carbon monoxide and methane such as the partial condensation process or processes for separating mixtures containing carbon monoxide and nitrogen only as principal components or processes including a nitrogen wash unit.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

Dans un procédé de production d'oxyde carbonique gazeux par distillation cryogénique, un gaz d'alimentation (1), contenant au moins de l'oxyde carbonique en tant que composant principal et au moins d'autres composants choisis parmi méthane, azote et hydrogène, est purifié par une étape d'adsorption dans un d'au moins deux lits adsorbants (3) en vue de la production d'un gaz d'alimentation purifié destiné à être envoyé à l'unité de séparation comprenant au moins une colonne de distillation (7, 19, 27). L'unité de séparation sépare le gaz d'alimentation pour produire de l'oxyde carbonique gazeux et l'oxyde carbonique gazeux est comprimé dans un compresseur de produit (35) en vue de la production d'un produit final à une pression de produit, la réfrigération étant assurée dans le process par un cycle de refroidissement de l'oxyde carbonique dans lequel un fluide de cycle est comprimé dans au moins le compresseur de produit, refroidi et détendu, au moins une partie de l'oxyde carbonique est liquéfiée pour former de l'oxyde carbonique liquéfié sous pression et une partie de l'oxyde carbonique liquéfié sous pression (51 A, 53A, 59A) est vaporisée à la pression de produit pour former un flux auxiliaire sous pression qui est ensuite mélangé au produit final, la vaporisation de l'oxyde carbonique ne s'effectuant qu'en cas d'augmentation de la demande en oxyde carbonique sous pression.
PCT/EP2012/062020 2011-06-24 2012-06-21 Procédé et installation de production d'oxyde carbonique gazeux par distillation cryogénique WO2012175635A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201280030991.7A CN104011488B (zh) 2011-06-24 2012-06-21 通过低温蒸馏供应气态一氧化碳的方法和设备

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
IN1810DE2011 2011-06-24
IN1810/DEL/2011 2011-06-24
EP11306060.2 2011-08-23
EP11306060A EP2562502A1 (fr) 2011-06-24 2011-08-23 Procédé et installation pour la fourniture d'un monoxyde de carbone gazeux par distillation cryogénique

Publications (2)

Publication Number Publication Date
WO2012175635A2 true WO2012175635A2 (fr) 2012-12-27
WO2012175635A3 WO2012175635A3 (fr) 2015-08-20

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FR3084453B1 (fr) * 2018-07-25 2020-11-27 Air Liquide Procede et appareil de separation cryogenique d'un melange de monoxyde de carbone, d'hydrogene et de methane pour la production de ch4
FR3133665B1 (fr) * 2022-03-21 2024-03-22 Air Liquide Procédé et appareil de séparation d’un mélange de monoxyde de carbone, de méthane et d’hydrogène

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EP1245533A1 (fr) 2001-03-21 2002-10-02 L'air Liquide, S.A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et dispositif pour le traitement de gaz de synthèse et de gaz apparentés
EP1479989A1 (fr) 2003-05-19 2004-11-24 L'Air Liquide S. A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et installation pour la production de monoxyde de carbone gazeux et/ou d'un mélange contenant de monoxyde de carbone

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FR2847568B1 (fr) * 2002-11-25 2005-02-11 Air Liquide Procede et installation de production d'un melange krypton/xenon a partir d'air
FR2861165B1 (fr) * 2003-10-20 2005-12-16 Air Liquide Procede et appareil pour la production de monoxyde de carbone et/ou d'hydrogene et/ou d'un melange d'hydrogene et de monoxyde de carbone par distillation cryogenique
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EP1245533A1 (fr) 2001-03-21 2002-10-02 L'air Liquide, S.A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et dispositif pour le traitement de gaz de synthèse et de gaz apparentés
EP1479989A1 (fr) 2003-05-19 2004-11-24 L'Air Liquide S. A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et installation pour la production de monoxyde de carbone gazeux et/ou d'un mélange contenant de monoxyde de carbone

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EP2562502A1 (fr) 2013-02-27
CN104011488A (zh) 2014-08-27
WO2012175635A3 (fr) 2015-08-20

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