EP2149021B1 - Aufbewahrungsgehäuse, verfahren und vorrichtung zur herstellung von kohlenmonoxid und/oder wasserstoff durch kryogene trennung, einschliesslich solch eines gehäuses - Google Patents

Aufbewahrungsgehäuse, verfahren und vorrichtung zur herstellung von kohlenmonoxid und/oder wasserstoff durch kryogene trennung, einschliesslich solch eines gehäuses Download PDF

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Publication number
EP2149021B1
EP2149021B1 EP08805790.6A EP08805790A EP2149021B1 EP 2149021 B1 EP2149021 B1 EP 2149021B1 EP 08805790 A EP08805790 A EP 08805790A EP 2149021 B1 EP2149021 B1 EP 2149021B1
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EP
European Patent Office
Prior art keywords
liquid
column
carbon monoxide
enclosure
discharging
Prior art date
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EP08805790.6A
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English (en)
French (fr)
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EP2149021A2 (de
Inventor
Alain Briglia
Arthur Darde
Natacha Haik-Beraud
Antoine Hernandez
Guillaume Teixeira
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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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Publication of EP2149021A2 publication Critical patent/EP2149021A2/de
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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
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F25J5/005—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger in a reboiler-condenser, e.g. within a column
    • 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
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2270/24—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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the present invention relates to an apparatus and a process for producing carbon monoxide and / or hydrogen by cryogenic separation.
  • this capacity is divided into several pots, which possibly hinders the flexibility of operation. In other units, this capacity is dedicated, which implies the need for additional equipment.
  • the present invention proposes to solve these problems, while having other advantages.
  • the condenser is bathed in cryogenic liquid, it overflows around the condenser over a hydraulic guard internal to the pot, the reserve of liquid is in the crown around this hydraulic guard. There is therefore only one equipment under pressure.
  • US Patent 4606745 describes an apparatus according to the preamble of claim 1.
  • the second part is supplied with liquid only by the overflow of liquid from the first part.
  • the distillation column is located outside the enclosure.
  • a single capacity serves at least two functions: on the one hand it stores an "independent" cooling reserve and on the other hand it is necessary for an element of the process (condenser, exchanger thermosiphon, etc.).
  • This capacity can be fed by all the currents producing liquid in the cold box.
  • the capacity is fed by at least two high-pressure flows through the reboilers, the high-pressure flow bypassing them. It can be powered by other flows, at different pressures.
  • the fact of gathering all the currents in a single capacity brings a great flexibility if different cases of march are to be considered, rather than attributing to each high pressure fluid one or more uses low pressure (thermosiphon, condenser, etc.). In addition to flexibility, we also gain in standardization. If the pressure of the capacity allows it, all the liquid needs can thus pass through this capacity.
  • the overflow makes it impossible to regulate the condensing power (in the example) by the liquid level, however, it is possible to regulate the energy exchanged in the condenser by adjusting the pressure of the capacity.
  • the liquid reserve makes it possible to regulate the level by turbine or by flow rate. This also allows to have a reserve of liquid to operate the device when the turbine is down and before starting the bottle feeding nitrogen spray.
  • Figure 1 represents a capacity and a column according to the invention
  • Figures 2 to 4 schematically represent apparatus for producing carbon monoxide by cryogenic separation according to the invention.
  • a column 1 is surmounted by a head condenser 3 fed with a gas overhead of the column. This gas condenses at least partially in the condenser 3 and is returned to the top of the column.
  • the condenser 3 is surrounded by a cylindrical barrier 5 sealingly attached to the bottom of a cylindrical chamber 21 enclosing the condenser.
  • the barrier and the enclosure are substantially concentric with the condenser 3.
  • the barrier 5 is lower than the enclosure 21.
  • the barrier may comprise cutouts at the top of the wall for the passage of liquid.
  • the barrier divides the enclosure into two parts A and B, the first part A being between the condenser and the barrier 5 and the second part B being located between the barrier 5 and the wall of the enclosure 21.
  • Pipes 15, 17, 19 feed the first part A and a pipe 7 is attached to the second part B, then being divided into lines 9, 11.
  • the condenser In use, the condenser is fed with liquid from at least one of the lines 15, 17, 19. This liquid is partially vaporized and the vapor thus formed is withdrawn from the chamber 21. When the liquid level reached the top of the barrier 5, the collected liquid overflows and falls in the second part B.
  • the illustrated capacity functions as described above and has the same structure as that described for the Figure 1 .
  • the process of Figure 2 is a methane scrubbing process comprising a K01 methane scrubbing column, a K02 depletion column, a carbon monoxide and KO3 methane separation column and a KO4 carbon monoxide and nitrogen separation column.
  • the flows fed to the columns and produced by the columns are not illustrated for the sake of simplification.
  • the method could include fewer columns or more columns.
  • the separation column of carbon monoxide and nitrogen is not an essential element of the invention.
  • the K01 column is fed with a feed rate
  • a fluid of the hydrogen depleted column is sent to the K02 exhaust column
  • the bottom liquid of the exhaust column is sent to the CO separation column.
  • CH 4 K03 and the column K04 is fed with a fluid from column K03, allowing the production of pure carbon monoxide in the bottom of column K04.
  • the capacitor C is fed with a liquid 21 coming from at least two different sources but having substantially the same composition. This liquid is rich in carbon monoxide.
  • the liquid 15 sent in the first part of the chamber comes from the reboiler Q6 of the exhaust column K02.
  • the liquid 17 sent in the first part of the chamber comes from the reboiler Q7 of a carbon monoxide and methane separation column.
  • the liquid 19 sent in the first part of the chamber comes from the exchanger 49.
  • the liquid overflowing over the barrier is divided into three parts.
  • Part X is sent via 7A and 9 to a cooling exchanger of the washing column K01.
  • Part Y is sent via 7A and 11 to a pot 41 and then to the main exchange line where the mixture feeding the apparatus cools.
  • Part 12 is sent to the head condenser Z of the CO / nitrogen separation column K04.
  • Part X evaporates in the cooling exchanger to form a flow 39. It is mixed with the vaporized flow rates 25, 37 from the condensers of column K03 and column K04 respectively.
  • the mixed flow 43 joins the overhead gas of the separator pot 41 and heats up in the exchanger 51.
  • This flow 43 is compressed by a compressor C1.
  • a compressed portion 45 is sent to the exchanger 49 and then is divided, the portion 31 feeding the column K04 and the remainder constituting the flow 19.
  • the remainder of the flow 43 is compressed in the compressor C2 to form part of the flow 47 which, cooled in the exchanger 51, becomes the flow 15 for the capacity C.
  • the compressor C3 compresses the rest of the flow to form the flow 49 which is divided in two. Part of the flow mixes with flow 47 and the remainder becomes flow 17.
  • the illustrated capacity functions as described above and has the same structure as that described for the Figure 1 .
  • the process of Figure 3 may be a partial condensation or methane scrubbing process comprising at least one depletion column, a carbon monoxide and methane separation column and a carbon monoxide and nitrogen separation column.
  • the apparatus comprises a methane scrubbing column.
  • the capacitor C is fed with a liquid 23 coming from at least two different sources but having substantially the same composition.
  • This liquid may for example be a liquid rich in carbon monoxide, rich in nitrogen or a mixture containing mainly hydrogen and carbon monoxide.
  • the liquid 15 sent in the first part of the chamber comes from the reboiler Q6 of a depletion column.
  • the liquid 17 sent in the first part of the chamber comes from the reboiler Q7 of a carbon monoxide and methane separation column.
  • the liquid 19 sent to the first part of the enclosure comes from the reboiler Q8 of a carbon monoxide and nitrogen separation column, if there is one.
  • the liquid 7 having overflowed over the barrier is divided into three parts 9, 11, 12.
  • the part 9 is sent to a cooling exchanger X of a washing column, if there is one.
  • Part 11 is sent to the main exchange line Y where the mixture feeding the apparatus cools.
  • Part 12 is sent to the head condenser Z of a column other than column 1, for example a carbon monoxide and nitrogen separation column, such as column K04 of the Figure 2 .
  • Each of these portions 9, 11, 12 vaporizes and is mixed with the vaporized liquid from the condenser 3.
  • the mixed flow forms a cycle gas which is compressed in a multi-stage compressor, called C1, C1 'and C2 compressors. , connected in series.
  • the compressor Cl compressed the gas to form a flow 45 which becomes the flow 19 downstream of the reboiler Q8.
  • the compressor C2 produces a flow 49 which feeds the reboilers Q6, Q7, the remainder 145 forming the flow 20 is also sent to the condenser 3.
  • the method of the Figure 4 represents a process for producing carbon monoxide and hydrogen by partial condensation.
  • the apparatus comprises a separator pot 405, a depletion column 411 and a carbon monoxide and nitrogen separation column 1.
  • Column 1 comprises a storage capacity according to the invention.
  • Part of the synthesis gas is used to reboil the depletion column 411 by means of the reboiler 405.
  • the gas of The partially condensed synthesis exits the exchange line 403 and is sent to the separator pot 405.
  • the overhead gas 407 heats up in the exchange line and serves as a hydrogen-rich product.
  • the liquid 409 is sent to the top of the depletion column 411.
  • the overhead gas 410 of the depletion column 411 leaves the apparatus after heating in the exchange line 403.
  • the tank liquid 415 of the column depletion 411 is sent to an intermediate point of the exchange line 403 where it cools and is divided into two.
  • Part 419 is sent to separation column 1 after expansion.
  • the remainder 417 heats up in the exchange line and is sent to the separation column 1 at a lower level.
  • the tank liquid 449 of the separation column 1 is sent to the head condenser thereof where it partially vaporizes.
  • the vaporized liquid rich in carbon monoxide 425 is sent to the exchange line 403 to heat up and then to the compressor C1.
  • Carbon monoxide is cooled with water.
  • a portion 453 serves as a product after a compression step in the compressor C2.
  • the rest 451 cools in the exchange line.
  • a portion 431 is expanded in a turbine T to provide frigories at separation and recycled to the compressor C1.
  • the rest 433 is divided in two.
  • Part 435 is sent to an intermediate temperature of the exchange line 403 at the bottom of the column 1 and at the top condenser (flow 437) after cooling in the exchanger 451 against a flow of liquid nitrogen 441.
  • the remains 453 is sent to the condenser at the temperature of the cold end of the exchange line 403.
  • the compressed cycle gas in the compressor C1 may be a carbon monoxide rich gas, a nitrogen rich gas, or a gaseous mixture of hydrogen and carbon monoxide.

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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)
  • Carbon And Carbon Compounds (AREA)

Claims (14)

  1. Gerät zur Herstellung mindestens eines Fluids durch kryogene Trennung, umfassend eine Destillationskolonne,
    wobei die Kolonne eine Flüssigkeitsspeicherkapazität (C) aufweist, wobei die Flüssigkeitsspeicherkapazität (C) ein Gehäuse (21), einen innerhalb des Gehäuses angeordneten Wärmetauscher (3), eine Sperre (5), die das Gehäuse in zwei Teile unterteilt, wobei sich der Wärmetauscher in dem ersten Teil (A) befindet, und wobei der zweite Teil (B) um den ersten Teil herum angeordnet ist, wobei die Sperre eine Höhe hat, die zumindest an bestimmten Punkten geringer als die Höhe des Gehäuses ist, um den Durchgang von Flüssigkeit von dem ersten Teil zu dem zweiten Teil über die Sperre zu ermöglichen, wenn die Kapazität im Dienst ist, und gegebenenfalls auf dichte Weise am Boden des Gefäßes befestigt ist, Mittel (15, 17, 19) zum Leiten der Flüssigkeit zu dem Inneren des ersten Teils des Gehäuses sowie Mittel (7) zum Entnehmen der Flüssigkeit aus dem zweiten Teil des Gehäuses und Mittel zum Leiten eines Fluids zu dem Austauscher und zum Entnehmen eines Fluids aus dem Austauscher umfasst, wobei der Austauscher ein Verdampfungssumpf oder ein Kopfkondensator ist,
    dadurch gekennzeichnet, dass das Gerät ein Gerät zur Herstellung von Kohlenmonoxid- und/oder Wasserstoff ist, und dass die Kolonne eine Kolonne zur Trennung von Kohlenmonoxid und Methan (K03) oder eine Kolonne zur Trennung von Kohlenmonoxid und Stickstoff (K04) ist.
  2. Gerät nach Anspruch 1, umfassend Mittel (15, 17, 19, 449, 451, 453) zum Leiten von der Flüssigkeit zu dem Inneren des ersten Teils, die aus mindestens zwei verschiedenen Quellen stammt, und/oder Mittel (7, 7A, 11, 12) zum Entnehmen von der Flüssigkeit aus dem zweiten Teil und anschließenden Leiten derselben an zwei verschiedene Bestimmungsorte.
  3. Gerät nach Anspruch 2, umfassend eine Waschkolonne (K01) und Mittel zum Leiten der entnommenen Flüssigkeit zumindest zu dem Kühler (X) der Waschkolonne.
  4. Gerät nach Anspruch 2 oder 3, umfassend eine Austauschleitung (51), Mittel zum Leiten von dem Fluid zur Versorgung des Geräts zu der Austauschleitung, um es dort zu kühlen, und Mittel (11) zum Leiten der entnommenen Flüssigkeit zumindest zu der Austauschleitung.
  5. Gerät nach Anspruch 2, 3 oder 4, umfassend Mittel zum Leiten der entnommenen Flüssigkeit mindestens zu einem Kondensator des Kopfs der Kolonne zur Trennung von Kohlenmonoxid und Methan oder der Kolonne zur Trennung von Kohlenmonoxid und Stickstoff.
  6. Gerät nach Anspruch 2, umfassend eine Entleerungskolonne (K02, 411, 511), die einen Verdampfungssumpf und Mittel (15) zum Leiten der kondensierten Flüssigkeit in den Verdampfungssumpf zu dem ersten Teil der Kapazität hat.
  7. Gerät nach einem der Ansprüche 2 bis 6, umfassend eine Kolonne zur Trennung von Kohlenmonoxid und Stickstoffmonoxid (K04), die einen Verdampfungssumpf und Mittel zum Leiten der kondensierten Flüssigkeit zu dem Verdampfungssumpf in dem ersten Teil der Kapazität hat.
  8. Gerät nach einem der Ansprüche 2 bis 7, umfassend eine Kolonne zur Trennung von Kohlenmonoxid und Methan (1), die einem Verdampfungssumpf (521) und Mittel (17) zum Leiten der kondensierten Flüssigkeit in den Verdampfungssumpf zu dem ersten Teil der Kapazität hat.
  9. Gerät nach einem der Ansprüche 2 bis 8, umfassend eine Austauschleitung (51, 403, 503) und Mittel (435, 437, 535, 537), um eine Flüssigkeit von der Austauschleitung zu dem ersten Teil der Kapazität zu leiten.
  10. Gerät nach Anspruch 1, wobei die Sperre eine im Wesentlichen zylindrische Form hat.
  11. Gerät nach Anspruch 1, wobei die Sperre koaxial zu dem Gehäuse ist.
  12. Verfahren zur Herstellung von Kohlenmonoxid und/oder Wasserstoff durch kryogene Trennung in einem Gerät nach Anspruch 1.
  13. Verfahren nach Anspruch 12, wobei die Flüssigkeit, die aus mindestens zwei verschiedenen Quellen stammt, in das Innere des ersten Teils geleitet wird.
  14. Verfahren nach Anspruch 12 oder 13, wobei die Flüssigkeit aus dem zweiten Teil entnommen wird, um sie dann an zwei verschiedene Bestimmungsorte zu schicken.
EP08805790.6A 2007-05-21 2008-05-16 Aufbewahrungsgehäuse, verfahren und vorrichtung zur herstellung von kohlenmonoxid und/oder wasserstoff durch kryogene trennung, einschliesslich solch eines gehäuses Active EP2149021B1 (de)

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FR0755165A FR2916523B1 (fr) 2007-05-21 2007-05-21 Capacite de stockage, appareil et procede de production de monoxyde de carbone et/ou d'hydrogene par separation cryogenique integrant une telle capacite.
PCT/FR2008/050843 WO2008142349A2 (fr) 2007-05-21 2008-05-16 Capacite de stockage, appareil et procede de production de monoxyde de carbone et/ou d'hydrogene par separation cryogenique integrant une telle capacite

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US20100199718A1 (en) 2010-08-12
FR2916523A1 (fr) 2008-11-28
WO2008142349A2 (fr) 2008-11-27
WO2008142349A3 (fr) 2013-07-18
FR2916523B1 (fr) 2014-12-12
EP2149021A2 (de) 2010-02-03
US8783062B2 (en) 2014-07-22

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