WO2001080981A1 - Trennung von fluidgemischen mittels membranisierter sorptionskörper - Google Patents
Trennung von fluidgemischen mittels membranisierter sorptionskörper Download PDFInfo
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- WO2001080981A1 WO2001080981A1 PCT/EP2001/004527 EP0104527W WO0180981A1 WO 2001080981 A1 WO2001080981 A1 WO 2001080981A1 EP 0104527 W EP0104527 W EP 0104527W WO 0180981 A1 WO0180981 A1 WO 0180981A1
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- membrane
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- separation
- porous
- soφtionsköφer
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- 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
- B01D53/22—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 diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
Definitions
- the present invention relates to a device and a method for separating fluid mixtures and a method for increasing the performance of membranes or membrane-like gas separation systems.
- Liquid, gaseous and vaporous fluid mixtures can be separated on membranes. Liquid mixtures of substances are separated on membranes by means of pertraction, one component of the liquid mixture being retained by the membrane, while a second component of the mixture passes through the membrane. The permeate on the back of the membrane is absorbed and discharged by a liquid phase.
- concentration gradients of the permeable or permeating substance through the membrane are the driving force for the permeation.
- the mechanisms mentioned above differ significantly. While the selectivity of Mechanism 1 is generally very low, the selectivity of Mechanism 2 depends on the exact adjustment of the pore size in the membrane, which places considerable demands on the production of such molecular sieve membranes.
- the limiting factor in this mechanism is, above all, the partial condensation pressure of the component to be separated, which in turn depends on the temperature of the system, which is why the smallest possible pores in the subnano range must be present, so that the separation operation can only be carried out here under restricted external conditions. Furthermore, a very homogeneous pore distribution is necessary here, which is not easy to produce in this pore size range.
- the fourth mechanism is the most flexible with regard to the external separation conditions, but places high demands on the composition of the membrane, since its adsorption capacity essentially determines the selectivity.
- Conventional two-layer membrane systems of the prior art consist of an active separation layer and a porous support layer. These membranes are designed either as a composite membrane or as an asymmetrical membrane.
- a thin, active separating layer is applied to a porous carrier layer, wherein the porous carrier layer can in turn consist of one or more porous layers.
- Asymmetric membranes are generally porous polymer systems that are subsequently modified so that a thin, homogeneous active separation layer forms on one side of the membrane.
- the concentration gradient required which forms the driving force for the mass transfer of the permeating component, is generated in the membrane separation processes known in the prior art in that a vacuum or vacuum prevails on the rear side of the membrane separation layer and / or an overpressure is applied on the loading side of the membrane ,
- the process temperature in such pressure-operated membrane systems is usually as low as possible, since low temperatures generally have a positive effect on the selectivity of the separation.
- Adsorption membranes also have the particular disadvantage that they are sensitive to particularly strongly adsorbing components of the fluid mixture, which occupy and permanently block the adsorption sites on the pores. These strongly adsorbing components, for example the mostly unavoidable water vapor, are very difficult to remove at normal, technically applicable negative pressures, which is why the efficiency of such membrane systems decreases relatively quickly during operation. To avoid To solve this problem, gas mixtures to be separated have to be pre-dried or pre-cleaned.
- Membranes that function according to the separation mechanism of the pore condensation and the surface flow also clog relatively easily, since very large or difficult-to-desorb molecules can pass through the membrane, which no longer detach from the sorbent in the desorption step. These membranes tend to "fill up” from their desorption side, which eventually leads to clogging of the membrane.
- the object of the present invention is to provide a device and a method for the separation of fluid mixtures which can efficiently remove strongly adsorbed molecules from the membrane and which enables a cost-effective separation of individual components from fluid mixtures in a technically simple manner.
- Another object of the present invention is to provide a device for separating fluid mixtures which can be optimally used for a wide variety of separation tasks.
- Another object of the present invention is to provide a method for simple detoxification of continuously operated separation membranes.
- the object of the invention is achieved by a device for separating fluid mixtures, comprising a porous and sorptively acting body which is in direct contact with a separating layer on at least one of its outer surfaces, devices for asymmetrical heating for the targeted introduction of thermal desorption energy into the porous body .
- Devices for generating a pressure gradient as well as devices for removal through the separating layer of permeated substances, the separating layer consisting of polymers, carbon fibers and carbon-like and / or metallic materials and / or oxidic and non-oxidic ceramic materials and / or glasses.
- the process-related object is achieved according to the invention by a method for separating fluid mixtures from at least two components, which comprises the following steps: a) contacting a separation layer with one to be separated
- Fluid mixture in a first work area b) permeating at least one component through the separation layer into a sorption body; c) moving at least one component of the fluid mixture to be separated through regions of the sorption body acting like sorption channels into the desorption region of the sorption body, d) thermally assisted desorption of at least one component present in the desorption region into a second
- Another process-related aspect of the present invention relates to a process for increasing the selectivity and / or the permeability of membranes and / or gas separation systems with a membrane-like effect, at least one main component being preferred and at least one secondary component permeating at least partially through a separating layer and / or a membrane system and a main component at the selected pressure and temperature conditions has an at least 10 times shorter dwell time than a secondary component, the membrane and or the membrane-like gas separation system being heated asymmetrically in situ.
- the first working area is understood to be the space on the retentate or feed side with respect to a separating layer or membrane and the second working area is the space on the permeate side. It is preferred according to the invention if the two working areas are connected to one another in a substantially fluid-tight manner, so that individual fluid components can only change from the first to the second working area by permeation through the separating layer.
- asymmetrical heating of the sorption body is understood to mean that essentially only individual parts, areas or surfaces of the sorption body are selectively changed in their temperature, ie are heated or cooled. It is preferred that the asymmetrical heating to one Temperature rise in the permeate leads, which is at least 50% greater than that in the retentate, preferably at least 200% and particularly preferably at least 500%.
- An essential element of the present invention is the so-called
- Sorption This is a porous body, which is preferably made of a sorptive material.
- the sorption body is in contact with at least one of its outer surfaces with a separating layer, which selectively allows one or more components from a fluid mixture to pass from the outside of the separating layer into the sorbent.
- the permeate passing through the membrane is adsorbed, chemisorbed and / or absorbed in the pore system of the sorption body.
- the So ⁇ tionsSystem will preferably be dimensioned so that larger amounts of permeate can be taken up in its pore system and optionally stored.
- the body that looks soctive has several functions. On the one hand, it acts as a carrier for the separation layer, which gives it sufficient mechanical stability, on the other hand, the body, due to its so ⁇ tion properties, causes the separation layer to be freed of membrane toxins during operation of the fluid separation device, which the body removes from the separation layer and in its pore system records and stores.
- membrane toxins that is to say substances which are so strongly sorbed or retained on membranes that they block and inactivate the membrane surface, can be removed continuously during operation of the separating device in that the membrane is placed on a carrier body which acts in a socially effective manner is applied.
- the carrier body also causes substances that can contaminate and clog the membrane, presumably flow from the membrane separation layer into the carrier body via a surface flow mechanism and are stored in its micropore system in the long term. It could be observed that even strongly adsorbed substances firmly adhering to the membrane migrate continuously into the carrier body, and in this way the separating layer remains permanently free of membrane toxins.
- the substances on the inner surface of the so ⁇ tive body which are basically mobile but difficult to desorb, can flow away quickly from the membrane itself. This prevents those species from combining on the surface as a kind of condensate film, which then has a significantly lower vapor pressure than the individual species (compare Kelvin equation). Furthermore, the large inner surface of the so ⁇ tive body increases the effective exchange area between adsorbate and fluid phase and thus accelerates the effective rate of deodorization even of those species that are difficult to desorb.
- the driving force for the migration of the membrane toxins into the porous body has thermodynamic as well as kinetic reasons. From a thermodynamic point of view, the enthalpy of adsorption in the microporous system of the carrier body is higher than the surface or in the pores of the membrane. This is mainly due to the cage-like pores in the carrier, which allows stronger adsorption than the slit pores in the interface.
- the migration of membrane poisons into the carrier body is kinetically favored, since the collective superficial adsorbate flow in the direction of the lower concentration gradient, like the gas flow behind the membrane, even drives strongly adsorbed molecules to the edge of the deodorant.
- the So ⁇ tionskö ⁇ er supports the outflow of all permeates from the actual bottleneck of all membrane separation processes, the membrane, by a downstream surface flow or capillary flow of the permeated components. It provides a large exchange surface to enable an energetically favorable desorption and to prevent the permeates from condensing behind the membrane and thus lowering their vapor pressure. Furthermore, it represents a carrier for the separating layer or the membrane, which preferably realizes a maximum outer surface in relation to the volume.
- the device according to the invention can in principle be understood as a combination of conventional membrane separation processes with adsorption filters. While continuously operating conventional membrane separation processes remove the permeates that pass through selectively through negative pressure on the permeate side, thus separating the substances into permeate and retentate, adsorption filters filter out individual components from a fluid stream, which are held in the filter's pore system.
- adsorption filters are exhausted when the adsorption seats are completely occupied and must then be regenerated discontinuously by desorption. This regeneration is usually carried out by blowing in hot steam and subsequent drying of the adsorption material, vacuum desorption etc.
- the present invention advantageously combines the continuous separation of fluid mixtures on membranes with the simple thermal but discontinuous deso ⁇ tion possible with conventional adsorption filters. In this way, a continuously working material separation process is obtained, which does not require the desorption of permeates at high negative pressure and avoids their disadvantages.
- the device according to the invention / the method according to the invention is also particularly suitable for increasing the selectivity and / or the permeability of membranes and / or gas separation systems which act like membranes, with at least one main component being preferred and at least one secondary component being at least partially by means of a separating layer and / or
- Permeane membrane system and a main component at the selected pressure and temperature conditions has an at least 10 times shorter residence time than a secondary component, the membrane and or the membrane-like gas separation system being heated asymmetrically in situ.
- the device according to the invention for separating fluid mixtures is preferably constructed in such a way that a So ⁇ tionsgro ⁇ er of any external shape is preferably equipped on one side with a separating layer which is applied directly to the surface of the porous So ⁇ tionskö ⁇ ers or at least in direct contact, which enables a mass transfer between the separating layer and So ⁇ tionsgro ⁇ er , stands with him.
- the device is also constructed so that the outer side of the membrane separation layer facing away from the So ⁇ tionsgro ⁇ er can be brought into contact with a fluid mixture to be separated, but not permeating substances from the fluid mixture can be removed as retentate from the outside of the membrane.
- the device according to the invention allows the main component to be separated from the fluid mixture to be separated with almost no interference.
- the So ⁇ tionskö ⁇ er usable according to the invention consists in a preferred embodiment of a material that has sufficient electrical conductivity to allow the passage of electrical current through the So ⁇ tionskö ⁇ er.
- the So ⁇ tionskö ⁇ er consists of a material which has a correspondingly suitable ohmic resistance, so that when an electric current is passed through the So ⁇ tionskö ⁇ er, this undergoes at least partial, regional and / or complete heating according to the ohmic resistance heating.
- the So ⁇ tionsgro ⁇ er according to this preferred embodiment is equipped with suitable devices for passing electrical current, for example by direct connection to positive and negative electrodes attached to opposite sides of the body, which are connected to a power source.
- the So ⁇ tionskö ⁇ er can of course also be made of non-conductive material if the heating is carried out with alternative heating methods such as infrared or microwave radiation.
- a particularly preferred embodiment of the present invention comprises a So ⁇ tionsgro ⁇ er which is provided on almost the entire outer surface with a membrane separation layer, and the permeate is removed, for example, through holes in the interior of the So ⁇ tionsgro ⁇ ers.
- the membrane-coated outer surface of the So ⁇ tionskö ⁇ ers can preferably be designed lamellar.
- the So ⁇ tionskö ⁇ er consists of a material that is both porous and has so ⁇ tive properties.
- suitable So ⁇ tionskö ⁇ er are 10 ⁇ to 1 mm on average.
- So ⁇ tionsgro ⁇ er suitable according to the invention have a BET surface area of at least 1 m 2 / g, preferably of at least 10 m 2 / g and particularly preferably between 250 and 2000 m 2 / g.
- the BET surface area of So ⁇ tionskö ⁇ er invention is between about 750 and 2000 m 2 / g.
- Suitable materials for So ⁇ tionskö ⁇ er invention include, for example, activated carbon, sintered activated carbon, amo ⁇ hen, pyrolytic carbon, ceramics such as optionally doped silicon and aluminum oxides, zeolites (type A, Y, ZSM5), metal-doped zeolites, conductive polymers such as polydiacetylenes, polycarbazoles, carbon doped Silicone elastomers, Luvocom ® plastics, metal-doped polycarbonates, porous glass (quartz, Vycor ® ), etc. Particularly preferred are carbon-based So ⁇ tionskö ⁇ er, especially those made of sintered activated carbon, or from pyrolyzed paper materials.
- Such activated carbon-based So ⁇ tionskö ⁇ er can be made relatively easily in any form by known methods for the production of molded bodies from sinterable materials.
- So ⁇ tionskö ⁇ er invention can be used with almost any external shape, for example in the form of plates or tubes.
- Activated carbon molded parts are usually produced afterwards by pressing coal / binder mixtures, then sintering and steam activation.
- sintered activated carbon with a density of 0.2-1.8 kg / 1, preferably 0.4-1.0 kg / 1, and a BET surface area of greater than 100 m 2 / g is used as the So ⁇ tionsgro ⁇ ermaterial. preferably greater than 500 m 2 / g, more preferably greater than 800 m 2 / g, particularly preferably greater than 1000 m 2 / g and particularly preferably greater than 1200 m 2 / g.
- Activated carbon materials enable high surface mobility of adsorbed components. Furthermore, such activated carbon material is structurally particularly suitable for making bores for outflow channels.
- So ⁇ tionskö ⁇ er made of a pyrolyzed paper-containing basic matrix, which is folded, embossed and compacted in a suitable manner to ensure a So ⁇ tionsgro ⁇ er with the largest possible outer surface in the smallest space.
- Corresponding So ⁇ tionskö ⁇ er can be obtained by pyrolysis of a flat, paper-containing basic matrix, in particular a basic matrix made of polymeric fiber-containing materials, with the exclusion of oxygen at elevated temperature.
- the paper-like basic matrix can optionally be embossed with groove patterns before pyrolysis and / or compactly folded into packages in various geometric arrangements.
- the resulting So ⁇ tionskö ⁇ er can also be modified by chemical vapor deposition of volatile ceramic precursors or hydrocarbon compounds in order to obtain inherently rigid, membrane-coated and self-supporting So ⁇ tionskö ⁇ ersysteme with favorable pore properties.
- Preferred and preferred membrane-based soapy bodies based on pyrolyzed paper can be produced in accordance with the invention in the following simple and inexpensive manner:
- a suitable Fase ⁇ apier is mixed with glass and carbon fibers and impregnated with bitumen, tar aromatic resins and the like.
- Fase ⁇ apiere are those which consist essentially of natural, semi-synthetic and / or synthetic fiber materials.
- the fibrous materials ensure sufficient porosity in the compression occurring during the pyrolysis / carbonization.
- Suitable natural fibers include abaka, bamboo, hemp, cellulose, amylose, starch, polyoses, lignin, flax, hemp, jute, sisal, coconut, kenaf, ramie, rosella, sunn, urena, linen, cotton, kapok, and fibers from cereals - Straw, alfa or esparto grass, fique, henecen, manila, phormium, bagasse, linters and the like.
- Suitable semisynthetic fibers are selected from sulfate pulp, sulfite pulp, soda pulp, cellulose derivatives such as cellulose esters and ethers, cellulose acetate, alginate, viscose, copper silk, polyisoprene and the like.
- Suitable synthetic fiber materials are selected from homo- and copolymers of polyacrylonitrile, polyvinyl alcohol, polyethylene, polypropylene, polyamide, polyester, polyurethane, as well as glass fibers, glass microfibers and the like.
- a paper is selected from abaca long fiber paper, tea bag paper, linen paper, handmade paper, printing paper, filter paper, flow paper, wood-free paper, wood-containing paper, kraft paper, crepe paper, cardboard paper, cardboard, LWC paper, oil paper, overlay paper, wrapping paper, Recycled paper, synthetic paper, tissue and the like are used.
- Papers with a volume-related area of at least 1,000 m 2 / m 3 , preferably 10,000 m 2 / m 3 and particularly preferably 20,000 m 2 / m 3 are particularly suitable.
- Linen paper with a weight per unit area of approximately 20 g / m 2 , or also Abaka-Langfase ⁇ apier with a weight per unit area of approximately 12 g / m 2 is particularly preferred.
- a mixture of silicon oxide and aromatic resin can then be applied in a thin layer, for example a few ⁇ m thick, in the form of grooves or line patterns to the glass fiber side using screen printing or similar processes.
- the paper pretreated in this way is then embossed to produce a
- a groove structure in the form of parallel grooves.
- defined outflow channels result from the grooves, which enable optimal fluidization of the fluids on the feed side of the membrane and rapid material exchange on the permeate side.
- any other surface structuring for example depressions, knobs and the like, can be applied, which the person skilled in the art will choose accordingly.
- emboss diagonal grooves on the paper at a distance of approximately 100 nm, optionally on one side or on both sides of the paper sheet.
- Structural embossing on the permeate side which can be produced by means of embossing techniques known to those skilled in the art, for example by roller embossing, is particularly preferred.
- a fold package which is particularly suitable according to the invention preferably has several hundred folds.
- Such a fold package is placed in an oven and there with a suitable device e.g. suctioned off over the whole area by pumps or applied with a vacuum.
- a suitable device e.g. suctioned off over the whole area by pumps or applied with a vacuum.
- the double-fold package is placed under
- Inert gas for example N 2 , argon and the like, for a certain time, generally about 0.5 to 3 hours, depending on the size of the fold package, brought to an elevated temperature, for example 100 to 250 ° C.
- the aromatic resins harden, the top and bottom folds contract sealingly on the end faces until a relative vacuum of 50 to 500 mbar, preferably about 200 mbar, is reached.
- the double-fold package is carbonized between about 250 ° C. and 800 ° C. under an inert gas, the carbonization gases preferably being sucked off continuously. This takes around 2 to 8 hours, depending on the size of the fold package.
- the double-fold package is annealed at approximately 1000 ° C to 2000 ° C.
- silicon carbides and mixed silicon oxides and carbides form at the locations previously coated with silicon oxide, which, among other things, ensure sufficient mechanical stability and chemical inertness of the finished component.
- the tempered double-fold package is premembraneized or sealed in order to produce a So ⁇ tionsgro ⁇ er usable according to the invention.
- So ⁇ tionskö ⁇ er invention are provided on at least one outer surface with a suitable separating layer.
- the So ⁇ tionsgro ⁇ er itself is a membrane.
- Suitable separating layers include polymer membranes, for example made of PTFE, polyacrylonitrile copolymer membranes, cellulose and cellulose derivatives, such as cellulose acetate, cellulose butyrate, cellulose nitrate, viscose, polyetherimide, polyoctylmethylsilane, polyvinylidene chloride, polyamides, polyurea, polyethylenethane, polyacrylate, polyacrylate, polyacrylamide, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylamide, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate, polyacrylate
- Suitable separating layers on So ⁇ tionsgro ⁇ em ceramic membrane according to the invention for example made of glass, silicon dioxide, silicates, aluminum oxide, perovskite, bomitride, aluminosilicates, zeolites, titanium oxides, zirconium oxides, borosilicates, combinations of the aforementioned and the like can also include.
- metal membranes based on transition metals such as Pd, Pt, Cu, Ni, Co, Mn, Cr, Fe, Au and / or Ag and mixtures / alloys and the like is also practical according to the invention.
- So-called CVD processes are particularly suitable for the production of carbon membranes on molded or soapy bodies.
- a carrier in the case of the present invention the So ⁇ tionskö ⁇ er pleat package is treated with hydrocarbon-releasing compounds at high temperatures (cf. G. Savage, "Carbon-Carbon Composites", Chapman & Hall, London, 1993, page 85 ff, US 3,960,769 , and US 3,979,330).
- hydrocarbon-releasing compounds Almost all known saturated and unsaturated hydrocarbons with sufficient volatility are suitable as hydrocarbon-releasing compounds. Examples include methane, ethane, ethylene, acetylene, linear and branched alkanes, alkenes and alkynes with carbon numbers of C ⁇ - 20 , aromatic hydrocarbons such as benzene, naphthalene etc., mono- and polylalkyl, alkenyl and alkynyl-substituted aromatics such as, for example Toluene, xylene, cresol, styrene etc. and the like. These are mostly reduced in CVD processes Concentration in an inert gas such as nitrogen, argon or the like is used. It is also possible to add hydrogen and / or water vapor to corresponding separating gas mixtures.
- Membraneization a further sintering step can be carried out at temperatures up to 2000 ° C in order to further stabilize the homogenization and strength.
- CVI processes essentially the same hydrocarbon-releasing compounds mentioned above are used as for CVD processes.
- the pore system can be subsequently expanded by briefly wetting the membrane with an oxidizing agent, for example nitric acid, and then post-treating it thermally.
- an oxidizing agent for example nitric acid
- a mixture of volatile hydrocarbons, preferably aromatic hydrocarbons, in particular benzene, and hydrogen is particularly preferably blown into the pleat package with a slight excess pressure and on the end side a gas mixture of inert gas, preferably nitrogen, and water vapor is blown in, which flows through the flow channels between the upper and lower folds.
- a gas mixture of inert gas preferably nitrogen, and water vapor is blown in, which flows through the flow channels between the upper and lower folds.
- mainly carbon is deposited, which seals the respective rows of folds and thus pre-membranes.
- the thickness of the resulting carbon membrane layer in the case of So ⁇ tionsgro ⁇ em usable according to the invention is up to 2 mm, preferably up to 100 microns, particularly preferably up to 10 microns.
- catalytically active metals can also be incorporated into the carbon membrane, in particular noble metals such as ruthenium, osmium, rhodium, iridium, palladium, platinum, silver, gold; and / or iron, cobalt, nickel and copper to increase the selectivity of separation of the membrane.
- noble metals such as ruthenium, osmium, rhodium, iridium, palladium, platinum, silver, gold; and / or iron, cobalt, nickel and copper to increase the selectivity of separation of the membrane.
- an electrical voltage is then applied in an optional fifth and final temperature treatment stage at approximately 500 to 900 ° C. to the upper and lower folds of the fold package.
- nitrogen is blown in on the face side, and nitrogen is blown in with 10% water vapor on the face side.
- a short-circuit current occurs at the remaining electrically conductive contact points between the upper and lower folds, which heats this contact point to temperatures at which carbon is oxidized by water vapor and is thus broken down into gaseous CO and / or CO 2 .
- SiO 2 , glass or SiC remains in the mechanical contact area between the top and bottom folds, which mechanically and chemically stabilizes the component.
- the finished So ⁇ tionskö ⁇ er membrane with a carbon membrane is allowed to cool.
- the membrane-shaped So ⁇ tionskö ⁇ er as described above, is formed in the form of a membrane package from pyrolyzed paper-like raw materials.
- the skilled person will be aware that almost any other geometry or shape of the So ⁇ tionskö ⁇ ers can also be used according to the invention.
- the folded membrane package is particularly preferred since it enables the largest possible membrane surface in the smallest space.
- the device according to the invention is preferably constructed from an embossed fold structure, the fold density being between 1 and 1000 folds per cm, preferably between 10 and 100 folds per cm.
- Embossed flow channels are also preferred, the minimum distance between them in the membrane plane being between 1 ⁇ m and 5 cm, preferably between 10 ⁇ m and 5 mm.
- the membrane package is produced by multiple folding of a fibrous paper matrix into a compact fold package, subsequent pyrolysis with the exclusion of oxygen and membrane treatment using CVD-deposited carbon as described above.
- So ⁇ tionskö ⁇ er is a root structure that is produced from an embossed and folded fabric.
- Carbon fiber membranes can also be used according to the invention.
- Carbon fiber membranes can, for example, according to the method of Soffer et al. (US 5,925,591) easily produced by pyrolysis of hollow cellulose fibers.
- Soffer et al. US 5,925,591
- a cellulose fiber layer is applied to the porous So ⁇ tionskö ⁇ er and optionally heated to pyrolysis after a drying step, Lewis acids or volatile salts, which act as carbonation catalysts, are sometimes added during the catalysis.
- modules made of hollow fiber membranes it is preferred if they are also heated asymmetrically according to the invention.
- An example of the combination of activated carbon with metal membranes is the reaction of methanol with water vapor, the device according to the invention using a palladium-coated So ⁇ tionskö ⁇ er made of activated carbon, and the H 2 formed passes through the Pd / carbon membrane.
- the pore system can also be subsequently expanded by briefly treating the membrane with an oxidizing agent, e.g. ENT, wetted, and then thermally treated.
- an oxidizing agent e.g. ENT
- the pore sizes of membranes which can be used according to the invention vary within a wide range.
- the pore sizes of such carbon molecular sieve membranes are correspondingly large, for example for the separation of gases generally up to 7 ⁇ im Diameter.
- the pores of corresponding membranes which can be used according to the invention can be in the range of the microporosity mentioned, ie with diameters of ⁇ 20 ⁇ .
- Membranes with average pore sizes of 3 to 20 ⁇ are preferred, particularly preferably 3 to 7 ⁇ .
- the inventive method for separating fluid mixtures by means of the So ⁇ tionskö ⁇ ervvoriques is such that the fluid mixture to be separated is applied to the outside of the separation layer, and individual components of the fluid mixture pass through the separation layer in the porous So ⁇ tionskö ⁇ er. There the permeates are sorted in the pore system (adsorbed, chemisorbed and / or absorbed) and distributed by means of surface flow, due to the change of place of sorted species, diffusion and / or similar transport processes in the pore system of the So ⁇ tionskö ⁇ ers.
- components which reduce the permeability of the separation layer flow into the So ⁇ tionskö ⁇ er for the purpose of in situ regeneration of the separation layer by direct contact of the separation layer and are temporarily stored there, and then transported to a deodorization area of the So ⁇ tionskö ⁇ ers, on which components are thermally supports desorb.
- the heating of parts of the So ⁇ tionskö ⁇ ers by means of suitable devices for introducing energy can also be done by electrical heating conductors, infrared radiators, induction heating, microwave heating, UV radiators, halogen rod heating, and / or passing hot fluid flows through the So ⁇ tionsgro ⁇ er.
- the devices for introducing energy used according to the invention can advantageously comprise catalysts arranged on the desorption side, which enable the oxidation of permeating organic substances, the catalysts comprising Pd, Cu, Ag, Pt or Ni, optionally on porous ceramic supports.
- the method according to the invention can be carried out in such a way that the temperature in the second working range is chosen to be less than, equal to or greater than in the first working range.
- the device and the method according to the invention are characterized in that means for generating and / or strengthening a concentration gradient with respect to at least one permeating component from the first to the second working area are provided in at least one of the working areas, these means consisting of cooling or heating devices, Means for generating low or excess pressure, electrical potentials and the like are selected.
- the method according to the invention is preferably carried out with a pressure gradient falling from the first to the second work area.
- the So ⁇ tionskö ⁇ er is on the permate side of the interface.
- the means for generating a concentration gradient comprise suitable cooling devices on the permeate side of the separating layer, which ensure continuous freezing-out, condensation of the permeate.
- Concentration gradients can be used advantageously.
- the retentate-side (first working area) use of excess pressure in membrane devices according to the invention is suitable for producing a concentration gradient that increases the permeate flow.
- Membrane optionally in combination with heating or cooling devices on the permeate side, can be used advantageously in preferred embodiments of the present invention.
- Applying an electrical potential gradient to the separation layer is particularly advantageous in order to generate a concentration gradient.
- the membrane device can generate an electrical potential gradient which can be regulated by means of suitable control devices, so that both the permeate flow and the selectivity of the membrane can be controlled accordingly.
- devices according to the invention achieve carbon tetrachloride loads of between 10 and 90% by weight, benzene loads of 3.2 g / m 2 or more at least 3% by weight, and iodine numbers of at least 1 mg / g, preferably of at least 75 mg / g.
- the fluid separation according to the invention can generally take place in the temperature range between minus 200 ° C. and plus 1000 ° C., the temperature to be selected depending on the device selected and the separation task to be carried out and can vary within wide ranges.
- the temperature required for the deodorization in the inventive So ⁇ tionskö ⁇ em in gas separations, pervaporation and vapor permeation is between - 200 and 300 ° C, preferably between 0 and 150 ° C. In individual cases, it is also possible to heat up to higher temperatures, up to 500 ° C. or more, in particular in the case of ceramic So ⁇ tionskö ⁇ em. In the case of separations in the condensed phase, temperatures in the range from 20 and 150 ° C. are generally preferred. The person skilled in the art will determine and determine the suitable temperature for the respective separation process by means of devices according to the invention by simple experiments.
- the device according to the invention and the method according to the invention can be adapted to a wide variety of separation tasks.
- both the general separation of gas mixtures into individual components such as that Oxygen production from air, hydrogen separation from process gases, the separation of CO 2 from natural gas, the separation of methane and / or CO 2 from hydrogen and the like are possible in a simple and cost-saving manner without being dependent on the application of strong negative pressure or pressure change methods.
- oxygen can be enriched, depending on the type of membrane used, up to 80% by weight, and in the case of high-temperature perovskite membranes even up to 99% by weight, oxygen permeating.
- the device according to the invention can also be used by selecting suitable materials for the So ⁇ tionskö ⁇ er and the membrane for the separation of liquid mixtures in pertractive processes or in pervaporation processes, as well as in steam permeation, dehumidification and / or disinfection of air and gases, supply or exhaust air filtration, etc.
- the internal heating of the filter enables both the sterilization and the in situ regeneration of the adsorbent. Even with a very low filtration requirement, the permeate can be drawn off discontinuously or the regeneration can also be carried out discontinuously.
- the So ⁇ tionskö ⁇ er also acts as an intermediate storage or reservoir for sorted substances.
- the removal of retentate from the first working area after a certain contact time and the permeate from the second working area can preferably be carried out in separate ways.
- the fluid mixtures can be brought into contact with further devices according to the invention, in the sense of a series connection of the membranes.
- the retentate already obtained can be used as a cycle gas for the discharge of further retentate in the first working area of a downstream and / or parallel connected membrane device, for example by recycling it.
- the permeate obtained from the second working area can be used to remove desorbed components from the second working area of a downstream and / or parallel connected membrane device.
- the parallel fluid flow routing to a large number of devices according to the invention with interposed cooling devices is also provided according to the invention.
- highly pure permeates or retentates can be obtained from fluid mixtures in the condensed and uncondensed phase.
- a device according to the invention can advantageously be used with a downstream pressure swing adsorption system
- Zeolite membrane (Zeolite PS A technology can be operated in order to obtain particularly highly enriched permeates even at low temperatures
- a perovskite membrane device can be connected downstream for further enrichment of oxygen in such separations.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Water Supply & Treatment (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2001578071A JP2003530999A (ja) | 2000-04-20 | 2001-04-20 | 成膜化した収着体を用いる流体混合物の分離 |
AU2001250427A AU2001250427A1 (en) | 2000-04-20 | 2001-04-20 | Separation of fluid mixtures using membranized sorption bodies |
EP01923730A EP1299175A1 (de) | 2000-04-20 | 2001-04-20 | Trennung von fluidgemischen mittels membranisierter sorptionskörper |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10019711A DE10019711A1 (de) | 2000-04-20 | 2000-04-20 | Trennung von Fluidgemischen mittels membranisierter Thermosorptionskörper |
DE10019711.6 | 2000-04-20 | ||
DE10019695.0 | 2000-04-20 | ||
DE10019695A DE10019695A1 (de) | 2000-04-20 | 2000-04-20 | Selbstreinigende Membranvorrichtung zur Trennung von Fluidgemischen |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2001080981A1 true WO2001080981A1 (de) | 2001-11-01 |
Family
ID=26005403
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2001/004527 WO2001080981A1 (de) | 2000-04-20 | 2001-04-20 | Trennung von fluidgemischen mittels membranisierter sorptionskörper |
Country Status (5)
Country | Link |
---|---|
US (1) | US20030101866A1 (de) |
EP (1) | EP1299175A1 (de) |
JP (1) | JP2003530999A (de) |
AU (1) | AU2001250427A1 (de) |
WO (1) | WO2001080981A1 (de) |
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WO2003070359A1 (en) * | 2002-02-19 | 2003-08-28 | L'air Liquide -Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Integrated membrane filter and its use for gas treatment |
WO2004082810A1 (de) * | 2003-03-18 | 2004-09-30 | Blue Membranes Gmbh | Membranplattenmodul |
DE10329535A1 (de) * | 2003-06-30 | 2005-03-24 | Sls Micro Technology Gmbh | Miniaturisierte Anreicherungsvorrichtung |
JP2007500589A (ja) * | 2003-07-31 | 2007-01-18 | ブルー メンブレーンス ゲーエムベーハー | 触媒活性単位を固定化するための支持体 |
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- 2001-04-20 US US10/258,335 patent/US20030101866A1/en not_active Abandoned
- 2001-04-20 WO PCT/EP2001/004527 patent/WO2001080981A1/de not_active Application Discontinuation
- 2001-04-20 AU AU2001250427A patent/AU2001250427A1/en not_active Abandoned
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Cited By (11)
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WO2003070359A1 (en) * | 2002-02-19 | 2003-08-28 | L'air Liquide -Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Integrated membrane filter and its use for gas treatment |
US6746513B2 (en) | 2002-02-19 | 2004-06-08 | L'air Liquide Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitations Des Procedes Georges Claude | Integrated membrane filter |
WO2004082810A1 (de) * | 2003-03-18 | 2004-09-30 | Blue Membranes Gmbh | Membranplattenmodul |
DE10329535A1 (de) * | 2003-06-30 | 2005-03-24 | Sls Micro Technology Gmbh | Miniaturisierte Anreicherungsvorrichtung |
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WO2012168154A1 (de) * | 2011-06-10 | 2012-12-13 | Süd-Chemie AG | Druckwechseladsorptionsverfahren |
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US9446344B2 (en) | 2011-06-10 | 2016-09-20 | Clariant Produkte (Deutschland) Gmbh | Pressure swing adsorption method |
Also Published As
Publication number | Publication date |
---|---|
US20030101866A1 (en) | 2003-06-05 |
JP2003530999A (ja) | 2003-10-21 |
AU2001250427A1 (en) | 2001-11-07 |
EP1299175A1 (de) | 2003-04-09 |
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