EP3227002A1 - Procédé de récupération d'eau par séparation d'un fluide de travail gazeux et séparateur d'eau destiné à un fluide de travail - Google Patents

Procédé de récupération d'eau par séparation d'un fluide de travail gazeux et séparateur d'eau destiné à un fluide de travail

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Publication number
EP3227002A1
EP3227002A1 EP15805392.6A EP15805392A EP3227002A1 EP 3227002 A1 EP3227002 A1 EP 3227002A1 EP 15805392 A EP15805392 A EP 15805392A EP 3227002 A1 EP3227002 A1 EP 3227002A1
Authority
EP
European Patent Office
Prior art keywords
reaction chamber
water
ionic liquid
working medium
outlet
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP15805392.6A
Other languages
German (de)
English (en)
Inventor
Robert Adler
Ekkehardt Klein
Markus Rasch
Christoph Nagl
Andreas POLLAK
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.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP3227002A1 publication Critical patent/EP3227002A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/0027—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions
    • B01D46/003—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions including coalescing means for the separation of liquid
    • B01D46/0031—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions including coalescing means for the separation of liquid with collecting, draining means
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/0027—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions
    • B01D46/0036—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions by adsorption or absorption
    • 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
    • B01D53/1412—Controlling the absorption process
    • 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
    • B01D53/1493—Selection of liquid materials for use as 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
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • B01D53/26—Drying gases or vapours
    • B01D53/263—Drying gases or vapours by absorption
    • 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
    • B01D53/26—Drying gases or vapours
    • B01D53/28—Selection of materials for use as drying agents
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/106—Removal of contaminants of water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/30—Ionic liquids and zwitter-ions
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0495—Composition of the impurity the impurity being water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/06—Heat exchange, direct or indirect
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/08—Drying or removing water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/12—Regeneration of a solvent, catalyst, adsorbent or any other component used to treat or prepare a fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/547—Filtration for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/58—Control or regulation of the fuel preparation of upgrading process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/60—Measuring or analysing fractions, components or impurities or process conditions during preparation or upgrading of a fuel

Definitions

  • the invention relates to a method for separating water from a gaseous working medium, and a water separator and a
  • Compressor stations for, for example, natural gas or hydrogen are basically designed for operation with a dry working gas. Will such a
  • Compressor station supplied with a hydrous working gas, so does the
  • the separation of the water components serves to prevent unwanted condensation in subsequent apparatuses and connecting pipelines.
  • an excessively high proportion of water is the result of subsequent use of fuel gases in internal combustion engines
  • Drying systems according to the prior art for example, work with
  • porous material such as silica gel.
  • Such highly porous materials absorb the water content from the working gas.
  • Beds in dryer systems of the prior art inherently require a very large volume.
  • a regeneration of the bed can be done by flowing with dry, unsaturated natural gas, heating or by exchanging the bed. To replace the bedding is at
  • the object according to the invention is achieved by a method for separating water from a gaseous working medium which has at least the following steps:
  • a reaction chamber is provided in which a
  • a substance mixture formed from a preferably used ionic liquid may contain a water content of> 0% by weight to ⁇ 100% by weight.
  • the reaction chamber is arranged such that a gaseous
  • Ionic liquids are (especially organic) salts whose lattice energy is so low that these salts are liquid in a temperature range of preferably -25 ° C to the point of their thermal decomposition, which is preferably greater than or equal to 250 ° C, without the Salt is dissolved in a solvent, such as water.
  • the ionic liquid can in particular
  • Methanesulfonate or ethanesulfonate (e.g., each wt% -50%), e.g. 1-ethyl-3-methylimidazolium methanesulfonate (CAS No .: 145022-45-3), tris (2-hydroxyethyl) methylammonium methylsulfate (CAS No .: 29463-06-7, also referred to as ethanaminium, 2-hydroxybenzyl) N, N-bis (2-hydroxyethyl) -N-methyl-, methylsulfate), or 1-ethyl-3-methylimidazolium ethylsulfate (CAS No .: 342573-75-5, also referred to as 1H-imidazolium, 1 - ethyl 3-methyl, ethyl sulfate).
  • the ionic liquid may be a mixture of the above ingredients, in particular CAS No .: 342573-75-5 and
  • Ionic liquids are thus able to bind water and to separate accordingly from the moist, gaseous working medium. Due to the low, barely measurable vapor pressure of the ionic liquids, the working medium in (at least constant) high purity after passing through the ionic liquid is available. In particular, particles are also deposited in the working medium and retained by the ionic liquid.
  • a particular advantage of this method is that the ionic liquid can be easily removed as a liquid material from the reaction chamber and can be easily cleaned or regenerated. In addition, a big advantage of this procedure is that the cleaning of the
  • Embodiment of the invention can be carried out under an atmospheric pressure, because the ionic liquid (technically) is incompressible and is mechanically insusceptible compared to a bed.
  • the ionic liquid technically
  • Embodiment is thus preferably held in the reaction chamber at least during the separation of water, an overpressure relative to the atmospheric pressure in an environment of the reaction chamber.
  • This is particularly preferred Process carried out in one stage. This is possible due to the low vapor pressure of the ionic liquid and the very high dissolving power of the ionic liquid.
  • the working medium is usually a gas or a two-phase fluid, in particular with a significantly larger proportion of gas, preferably greater than 90% by volume, whereby solid (contaminant) particles may also be contained.
  • Working medium is natural gas or hydrogen.
  • the method is carried out as a continuous process, wherein a working medium inlet for introducing the aqueous working medium and a clean medium outlet for discharging the dried working medium are provided, wherein preferably the working medium to be dried rises against the gravitational field by the ionic liquid upwards or . to be led.
  • Other ways of driving are however also conceivable.
  • the gaseous working medium is preferably continuously passed through the ionic liquid, so that this cleaning or drying of the working medium can be incorporated into a continuous (or quasi-continuous) process, and the working medium (quasi) continuously, for example, a compression ( in particular in a downstream compressor station) can be fed.
  • the working medium is supplied to the ionic liquid from below and, due to its lower density relative to the ionic liquid in the ionic liquid, rises upward against the gravitational field (the earth) therein and is discharged via the clean medium outlet above the liquid level of the ionic liquid.
  • the pure medium here is the dried and possibly freed from particles working medium.
  • the treatment can also be carried out as a separate process without the previously explained steps for separating water from a working medium.
  • the reaction chamber is also used for treatment (also called regeneration) of the ionic liquid, in which case preferably the implementation of the working medium is interrupted in order not to generate (large) losses of working medium.
  • the sufficiently loaded cleaning medium, ie the ionic liquid, is in the
  • Water outlet provided, which is preferably arranged above the ionic liquid, so that preferably substantially only vaporous water (due to the low vapor pressure of the ionic liquid) is removed.
  • the ionic liquid, or preferably a part of the ionic liquid, exchanged for processing wherein preferably the working medium for separating water can be continuously passed through the (remaining) ionic liquid.
  • the working medium for separating water can be continuously passed through the (remaining) ionic liquid.
  • as much purified ionic liquid is always supplied as is removed to be purified ionic liquid.
  • the ionic liquid is continuously exchanged, so that in particular the
  • Loading level of the ionic liquid can be kept substantially constant or within certain limits.
  • trapped particles may be continuously filtered out of the ionic liquid, for example by means of at least one filter downstream of the reaction chamber (e.g., in the conduits and / or in the treatment apparatus).
  • the distilled water obtained in the preparation is collected, preferably before the ionic liquid is freed by means of one or more filters of particles.
  • the recovered water is provided to another process.
  • the ionic liquid is previously freed from particles by means of one or more filters, so that a high-purity water distillate is obtained.
  • Reaction chamber for the deposition and regeneration use is preferably accomplished by means of alternately open pure medium outlet and water outlet, the capture of the water. With spatial separation of separation and treatment a continuous removal of water is possible.
  • a dead space in the reaction chamber is reduced to a desired level before starting the replacement of the ionic liquid by raising the liquid level, whereby a safety distance to the existing (upper) outlets can be taken into account (eg not to flood).
  • the dead space in the reaction chamber that is to say the space which is not filled with an ionic liquid, is preferably reduced to the extent that process reliability permits in particular. This will the volume in which the working medium is not treated, kept low, so that the volume efficiency of this method is very high, especially in comparison to beds.
  • the dead space prior to replacement and / or replacement of the ionic liquid, is either kept as low as possible or reduced as little as possible to avoid discharging (too) a large amount of working fluid during the cleaning process and thus losing it goes.
  • the dried working medium to be discharged is passed over at least one coalescing filter in order to carry out a fine separation of water fractions before it is removed as pure medium and made available to a subsequent process.
  • an atmospheric overpressure is maintained in the reaction chamber at least during the water absorption.
  • a water separator for a gaseous working medium which comprises at least the following
  • Components includes:
  • a liquid-tight reaction chamber for receiving a hygroscopic ionic liquid wherein in particular the reaction chamber is filled with the hygroscopic ionic liquid (which then forms part of the water separator), and wherein in particular the reaction chamber for
  • Carrying an overpressure is designed relative to the atmosphere surrounding the reaction chamber;
  • a lockable working medium inlet for introducing the gaseous and aqueous working medium to be dried in the reaction chamber, wherein in particular the working medium inlet below the reaction chamber is arranged;
  • shut-off clean medium outlet for removing the dried working medium from the reaction chamber
  • Puremediumauslass is arranged above the reaction chamber.
  • the water separator thus comprises a liquid-tight reaction chamber, which is preferably designed gas-tight beyond.
  • the (highly) hygroscopic ionic liquid is preferably contained or receivable in the reaction chamber, as has already been described at the outset.
  • the working medium inlet and the clean medium outlet face each other along a longitudinal axis of the reaction chamber along which
  • Reaction chamber extends or has a maximum extent, so that the treatment path of the working medium is as long as possible.
  • the clean medium outlet is arranged above the reaction chamber with respect to the gravitational field (of the earth) and the working medium inlet is arranged below the reaction chamber. That is, the longitudinal axis of the reaction chamber preferably extends along the vertical. However, the reaction chamber can also be aligned along the horizontal, so that the longitudinal axis is horizontal (and the working medium according to flows from left to right or vice versa).
  • the gaseous working medium which usually has a lower density than the ionic liquid, against the gravitational field in the ionic liquid automatically, so without supply of active energy to ascend, wherein at least a majority of the water content of the working medium is bound by the hygroscopic ionic liquid. Due to the already described above low vapor pressure of the ionic liquid thus occurs at the clean medium outlet, a (substantially) high-purity, dried working fluid from the ionic liquid, which can now be fed to another process.
  • the reaction chamber is preferably designed to carry pressure, so that the method can be carried out even with a significant overpressure relative to the surrounding atmosphere.
  • the water separator is preferably designed for carrying out a method as described above.
  • at least one water outlet is furthermore preferably provided or arranged above the reaction chamber, wherein evaporating water can be discharged via the water outlet during the treatment of the ionic liquid in the reaction chamber.
  • the reaction chamber may have a heating element, which for
  • At least one exchange outlet preferably below the reaction chamber, is provided, which is set up and provided for supplying and / or removing ionic liquid from the reaction chamber.
  • the ionic liquid can be discharged in particular from the reaction chamber, so that, for example, a treatment of the ionic liquid outside the reaction chamber can be carried out.
  • a supply and removal is particularly easy to carry out, for example by means of a liquid pump.
  • At least one inlet and at least one outlet are provided, by means of which the ionic liquid is continuously exchangeable.
  • the ionic liquid can be withdrawn via the outlet and at the same time - in regenerated form - be fed via the inlet into the reaction chamber.
  • the loading of the ionic liquid can thus be regulated with advantage and a continuous operation of the water separator is possible.
  • the water separator can thus be integrated with advantage into a continuous process structure.
  • the clean medium outlet has at least one coalescing filter on the reaction chamber side or is in flow connection with such a filter.
  • the coalescing filter is preferably designed for separating remaining water fractions from the dried working medium.
  • a water separator system for drying a gaseous working medium is proposed, wherein the
  • Water Separator system comprises at least one water separator according to the invention (for example, according to an embodiment described herein) and at least one separate treatment device, which is designed for conditioning (regeneration) of the ionic liquid so that it can be reintroduced into the reaction chamber.
  • the treatment device may have at least one particle filter for filtering out particulate impurities from the ionic liquid. Furthermore, the treatment device preferably has at least one heating element for heating the ionic liquid or for evaporating water bound to the ionic liquid. Furthermore, the treatment unit preferably has at least one water outlet for discharging the evaporated water.
  • the treatment device is preferably connected via at least one flow path to the reaction chamber, preferably via an inlet and an outlet of the reaction chamber, so that a continuous treatment of the ionic liquid is possible.
  • the ionic liquid is withdrawn via the outlet from the reaction chamber, regenerated in the treatment device and returned to the reaction chamber via the inlet.
  • the separation of water from the working medium in the reaction chamber in particular at pressures in the reaction chamber in the range of 1 bar (or 0 barü) to 551 bar (or 550 barü), in particular in the range of 20 bar to 330 bar, in particular in the range of 16 bar to 250 bar, and in particular at
  • the separation of water from the working medium is preferably at a temperature in the reaction chamber in the range of + 60 ° C to + 150 ° C and a pressure in the reaction chamber in Range from 20 bar to 330 bar instead. If the working medium is hydrogen or the
  • Working medium has hydrogen
  • the deposition of water from the working medium preferably takes place at a temperature in the reaction chamber in the range of + 60 ° C to + 160 ° C and a pressure in the reaction chamber in the range of 16 bar to 250 bar instead.
  • Fig. 2 a Wasserabscheidersystem with separate processing device.
  • a water separator 1 in which a reaction chamber 3 is provided, which with an ionic liquid 4 to a
  • Liquid level 18 is filled.
  • a heating element 10 projects, with which the ionic liquid 4 can be heated.
  • a working medium inlet 5 is provided, via which to be dried (water-containing) and gaseous working medium 2, preferably natural gas or hydrogen, is introduced into the reaction chamber 3.
  • a clean medium outlet 6 is provided on the upper side of the reaction chamber 3, which in this example is arranged in a cover 29 (see below) of the reaction chamber 3.
  • a dried working fluid 7 is discharged.
  • the reaction chamber 3 preferably extends in operation along a vertical longitudinal axis or cylinder axis, wherein the working medium inlet 5 and the clean medium outlet 6 lie opposite one another along the longitudinal axis.
  • Reaction chamber 3 may have a cylindrical, along the longitudinal axis extended
  • reaction chamber 3 can be closed at the bottom by a wall connected to the ground (except for any inlets and outlets).
  • the reaction chamber 3 is preferably closed by the cover or cylinder head 29, which can be screwed to the wall 8 via screw connections, of which only the screwing bores 23 are shown schematically here.
  • a water outlet 6 is provided above the reaction chamber 3, via the water vapor during the reprocessing of the ionic liquid 4, for example by means of heating the ionic liquid 4 by means of the heating element 10, can be discharged.
  • the clean medium outlet 6 and the water outlet 9 are preferably formed in the lid 29.
  • an exchange outlet 11 is arranged below the reaction chamber 3, via which the ionic liquid 4 can be supplied to the reaction chamber 3 and removed therefrom.
  • the clean medium outlet 6 can be shut off by means of the pure medium lock fitting 21, for example, when the ionic liquid 4 is conditioned (by heating).
  • the water outlet 9 can be shut off by means of a water-blocking valve 22, for example during the deposition phase when the water-containing working medium 2 is dried.
  • a coalescing filter 14 downstream of the reaction chamber 3 is fluidly connected to the clean medium outlet 6, which is arranged and provided for fine separation of the residual water content in the dried working medium 7. After that, a pure medium 20 can be fed to a subsequent process or storage.
  • the dead volume of the reaction chamber 3 is very low and in particular only to a safety distance 19 between the
  • the water separator 1 shown here is particularly compact and allows a continuous implementation of the water separation from the gaseous
  • a Wasserabscheidersystem 15 with a water separator 1 and a separate Aufleungsvorric device 16 is provided, wherein the water separator 1 is constructed similar to that shown in Fig. 1 and also preferred here
  • Chamber wall 8 is designed for an overpressure against the surrounding atmosphere.
  • an inlet 12 and an outlet 13 are provided on the reaction chamber 3, which thus form two exchange ports 11.
  • the inlet 12 allows the supply of ionic liquid 4, which is recycled from the processing device 16 can be fed.
  • the outlet 13 connects the water separator 1 and the treatment device 16, so that the ionic liquid 4, here for example by means of a pump 24, the treatment in the processing device 16 can be fed.
  • a particle filter 17 is provided downstream of the reaction chamber 3 or in the outlet 13, with which particles of the ionic liquid 4 introduced from the aqueous working medium 2 can be separated off.
  • In the conditioning device 16 is a heating element 10th
  • the ionizing liquid 4 can be heated via the treatment inlet 25, so that water is released in vapor form and as water vapor 28 via a water outlet 9 of the treatment device 16 can be discharged.
  • the dried ionic liquid is then poured over the
  • Treatment outlet 26 discharged and in turn fed via a return line 27 and the inlet 12 of the reaction chamber 3.
  • this water separation system 15 is particularly suitable for continuous processes in which a disruption of the water separation is normally not provided.
  • the method is carried out as possible in such a way that a water-containing, gaseous working medium 2 of the reaction chamber 3 from below via the
  • Reaction chamber 3 again, preferably cooled, supplied.
  • water is separated from a natural gas-containing working medium 2 using one of the ionic liquids described above, wherein the separation of water from the
  • water is from a
  • the separation of water from the working medium at a temperature in the reaction chamber 3 in the range of + 60 ° C to + 160 ° C and a pressure in the reaction chamber in the range of 16 bar is performed up to 250 bar.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Drying Of Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention concerne un procédé de récupération d'eau par séparation d'un fluide de travail gazeux (2), comprenant au moins les étapes consistant à : remplir une chambre de réaction (3) d'un liquide ionique hygroscopique (4) ; alimenter en fluide de travail (2) aqueux (2) et faire passer le fluide de travail (2) à travers le liquide ionique (4), l'eau se liant au liquide ionique (4) et se séparant ainsi du fluide de travail ; et évacuer le fluide de travail (7) déshydraté. L'invention concerne également un séparateur d'eau (1) correspondant et un système de séparation d'eau (15).
EP15805392.6A 2014-12-04 2015-12-01 Procédé de récupération d'eau par séparation d'un fluide de travail gazeux et séparateur d'eau destiné à un fluide de travail Withdrawn EP3227002A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102014017966.4A DE102014017966A1 (de) 2014-12-04 2014-12-04 Verfahren zum Abscheiden von Wasser aus einem gasförmigen Arbeitsmedium sowie ein Wasserabscheider für ein Arbeitsmedium
PCT/EP2015/002413 WO2016087039A1 (fr) 2014-12-04 2015-12-01 Procédé de récupération d'eau par séparation d'un fluide de travail gazeux et séparateur d'eau destiné à un fluide de travail

Publications (1)

Publication Number Publication Date
EP3227002A1 true EP3227002A1 (fr) 2017-10-11

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EP15805392.6A Withdrawn EP3227002A1 (fr) 2014-12-04 2015-12-01 Procédé de récupération d'eau par séparation d'un fluide de travail gazeux et séparateur d'eau destiné à un fluide de travail

Country Status (7)

Country Link
US (1) US20180290102A1 (fr)
EP (1) EP3227002A1 (fr)
JP (1) JP2017538571A (fr)
KR (1) KR20170091146A (fr)
AU (1) AU2015357759A1 (fr)
DE (1) DE102014017966A1 (fr)
WO (1) WO2016087039A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102016010000A1 (de) * 2016-08-18 2018-02-22 Linde Aktiengesellschaft Verfahren, Einrichtung und System zur Abscheidung von Wasser aus einer ionischen Flüssigkeit
JP6808192B2 (ja) * 2016-09-30 2021-01-06 国立研究開発法人産業技術総合研究所 乾燥水電解ガスの製造方法及びその装置
JP7495077B2 (ja) 2019-07-01 2024-06-04 国立研究開発法人産業技術総合研究所 乾燥水電解水素ガスの連続的製造方法及びその装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0211659A2 (fr) * 1985-08-12 1987-02-25 The Dow Chemical Company Procédé de séchage d'un gaz
DE102011121012A1 (de) * 2011-12-13 2013-06-13 Linde Aktiengesellschaft Verfahren zur Kohlenwasserstoffabtrennung
US20140314659A1 (en) * 2011-02-21 2014-10-23 Christopher L. Becker Hydrogen Purification Process

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1310543A1 (fr) * 2001-11-07 2003-05-14 Haldor Topsoe A/S Procédé de séchage d'un flux d'hydrocarbures
US7638058B2 (en) * 2005-04-07 2009-12-29 Matheson Tri-Gas Fluid storage and purification method and system
DE102010004779A1 (de) * 2010-01-14 2011-07-21 Heym, Florian, 95444 Verfahren zur Trocknung von Gasen
JP5585873B2 (ja) * 2010-09-03 2014-09-10 独立行政法人産業技術総合研究所 イオン液体を用いた環境浄化方法およびその装置
WO2012109550A1 (fr) * 2011-02-11 2012-08-16 Munters Corporation Appareil et procédé d'élimination de la vapeur d'eau se trouvant dans des rejets d'une usine de production

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0211659A2 (fr) * 1985-08-12 1987-02-25 The Dow Chemical Company Procédé de séchage d'un gaz
US20140314659A1 (en) * 2011-02-21 2014-10-23 Christopher L. Becker Hydrogen Purification Process
DE102011121012A1 (de) * 2011-12-13 2013-06-13 Linde Aktiengesellschaft Verfahren zur Kohlenwasserstoffabtrennung

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of WO2016087039A1 *

Also Published As

Publication number Publication date
US20180290102A1 (en) 2018-10-11
DE102014017966A1 (de) 2016-06-09
KR20170091146A (ko) 2017-08-08
JP2017538571A (ja) 2017-12-28
WO2016087039A1 (fr) 2016-06-09
AU2015357759A1 (en) 2017-06-22

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