EP2134434A1 - Method and device for treating liquids, using an electrolytic drying stage - Google Patents
Method and device for treating liquids, using an electrolytic drying stageInfo
- Publication number
- EP2134434A1 EP2134434A1 EP08735170A EP08735170A EP2134434A1 EP 2134434 A1 EP2134434 A1 EP 2134434A1 EP 08735170 A EP08735170 A EP 08735170A EP 08735170 A EP08735170 A EP 08735170A EP 2134434 A1 EP2134434 A1 EP 2134434A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- carrier gas
- steam
- water vapor
- liquid
- stream
- 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- Withdrawn
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/2881—Compression specifications (e.g. pressure, temperature, processes)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/22—Evaporating by bringing a thin layer of the liquid into contact with a heated surface
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/448—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by pervaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/46115—Electrolytic cell with membranes or diaphragms
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/33—Wastewater or sewage treatment systems using renewable energies using wind energy
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Definitions
- the invention relates to a method for the treatment of liquids according to the preamble of claim 1 and a device for the treatment of liquids according to the preamble of claim 30.
- At least a partial stream of a hot, laden with water vapor carrier gas as a hot water vapor carrier gas stream is subjected to a water vapor electrolysis, in the at least part of the Hydrogen and / or oxygen gas is split off from the hot water vapor carrier gas stream and a dried carrier gas stream is generated.
- the water vapor carrier gas stream preferably has a temperature between 70 ° to 300 0 C, preferably between 90 ° and 250 ° C and that at operating pressures or pressures between 1 bar and 11 bar absolute, depending on the currently prevailing operating conditions for a z , B. Wasseraufhneungsl.
- Wastewater treatment device which also corresponds to the operating conditions for the steam electrolysis, so that the hot water vapor carrier gas stream - in particular from a device for the treatment of liquids, in particular of sea and / or brackish water and / or a waste liquid and / or wastewater,
- the steam electrolysis according to the invention can be used for drying the water vapor carrier gas stream and thus for the generation of a dried carrier gas stream.
- Such a dried carrier gas stream can then be returned to the process, wherein this dried carrier gas stream with a significantly larger amount of z. B. can be reloaded aufrender liquid than would be the case without drying with the original hot water vapor carrier gas stream.
- the present inventive concept which is expressly claimed as an independent invention idea independently of the drying of the hot water vapor carrier gas stream by means of steam electrolysis, it is provided, at least a partial stream of a diverted from the carrier gas stream or derived, loaded with water Eduktstromes ( hot water vapor Eduktstrom) to undergo a steam electrolysis in which at least part of the hydrogen and / or oxygen from the hot water vapor Eduktstrom cleaved and a dried Eduktstrom is generated.
- the educt stream laden with steam is preferably a hot concentrate stream laden with steam, which is drawn off from a concentrate separator to which an overheated, wet carrier gas / vapor mixture is fed, as will be explained in more detail below.
- educt streams for the hydrogen or oxygen recovery in the context of a steam electrolysis which have been diverted or withdrawn from the carrier gas cycle.
- These are preferably educt streams or process streams which contain contaminants removed or removed in the course of the treatment of the liquids in certain treatment stations or treatment stages, in particular those impurities of the liquid which in turn represent valuable substances and are to be recovered.
- drying or drying of these process streams can thus be achieved, for which, owing to the water already present in vapor form, a significant reduction in the electrical energy required for the electrolysis is achieved. so that the recovery of valuable material can be carried out process-optimally with relatively little expenditure of energy.
- the invention has the advantage that with this z. B. from waste liquids can be recovered as treatment liquids pure hydrogen, which in turn can be fed to another use, for. As fuel for engines or internal combustion engines or as a coolant in power plants or other industrial plants, to show only a few uses.
- an electrolytic process in particular an alkaline electrolysis, such as.
- an alkaline pressure electrolysis proton exchange membrane electrolysis and high temperature electrolysis, both as autothermal and as an allothermal electrolysis process in question.
- the energy consumption for the gas drying according to the invention of a hot water vapor carrier gas stream and / or a hot steam original stream is only about 2.7 kWh / m 3 hydrogen, whereas the energy requirement for a conventional electrolysis for the production of hydrogen is essential is higher and depending on the electrolysis process between about 9 - 18 kWh / m 3 hydrogen.
- the hot water vapor carrier gas stream and / or the hot water vapor Eduktstrom is passed for steam electrolysis in a reaction space of a steam electrolyzer in which at least one anode and at least one cathode are arranged as electrodes, which are preferred is supplied by a rectifier as an energy supply device the still required electrical energy to split off the hydrogen and / or oxygen.
- the entire hot steam carrier gas stream and / or water vapor educt stream can be fed to the steam electrolysis.
- the steam electrolysis is supplied in accordance with predetermined parameters, in particular the gas drying degree and / or the hydrogen demand and / or the oxygen demand, predetermined amount of the hot water vapor carrier gas stream and / or the hot water vapor Eduktstromes. This can be done with respect to the energy consumption optimized gas drying or Edukttrocknung means of at least one steam electrolyser. So z. B. depending on z. B. Preparation process and required Gastrocknungsgrad z. B.
- the steam-electrolysis supplied amount of hot water vapor carrier gas and / or the hot steam Eduktstromes is set by means of a control device by means of a arranged in the supply line to a steam electrolyzer and coupled to the control device and / or Measuring device, which is formed in particular by a flow rate adjusting and measuring device, is controlled.
- the dried carrier gas stream and / or educt stream coming from the steam electrolysis via at least one measuring device is also preferred here guided, by means of which the content of hydrogen and / or oxygen in the dried carrier gas stream and / or in the dried Eduktstrom can be determined.
- This information is then provided to the controller as a parameter, e.g. B. as actual value parameter, so that the water vapor electrolysis to be supplied amount of hot water vapor carrier gas stream and / or the hot water vapor Eduktstromes can be determined in a simple and reliable manner.
- At least part of the hydrogen and / or oxygen obtained in the steam electrolysis be withdrawn from the steam electrolyser and stored in a gas storage, in particular in a compressed gas storage or cached.
- a suction and / or pumping device is preferably provided between the steam electrolyser and the respective compressed gas storage, which is preferably formed by a vacuum pump.
- a shut-off valve as a shut-off device and / or a check valve as a non-return valve is preferably arranged in the region of the respective compressed gas storage.
- the hydrogen and / or oxygen obtained in the steam electrolysis is supplied to a fuel cell, by means of which energy is generated, which in turn is in the treatment plant itself to support the local energy demand can be used directly. It is of course particularly preferred that in the context of steam electrolysis both hydrogen and oxygen are recovered, which can be supplied to the fuel cell. In principle, however, it is also possible to supply the hydrogen and / or the oxygen of the fuel cell at least partially from other sources.
- the hydrogen and / or oxygen obtained as part of the steam electrolysis is supplied to the fuel cell according to predetermined operating parameters by means of a control and regulating device at predetermined times and in predetermined amounts, so that an optimized operation of the fuel cell can be ensured.
- the hydrogen and / or oxygen obtained in the steam electrolysis is temporarily stored in a gas storage and the hydrogen and / or oxygen from these gas storage out of the fuel cell is supplied according to the predetermined operating parameters.
- the electrical energy obtained by means of the fuel cell is supplied to electrical consumers of the treatment plant, in particular z.
- electrical consumers of the treatment plant in particular z.
- steam electrolysers or the rectifiers of such water vapor electrolysers in addition or as an alternative to this, however, other electrical consumers, such as, for example, pumps, valves or the like, can also be supplied with energy by the fuel cell.
- other electrical consumers such as, for example, pumps, valves or the like, can also be supplied with energy by the fuel cell.
- it is also possible to supply the electrical energy gained from the fuel cell other uses, for. B. fed into a power grid or else to supply a thermal dryer, as used in accordance with a preferred embodiment of the present invention for concentrate drying, which will be explained in more detail below.
- a shut-off valve as a shut-off device and / or a non-return valve between the water vapor electrolyser and the respective suction and / or pumping device.
- Vacuum pump or compressed gas storage are each associated with those electrodes in which the gas to be sucked is formed.
- membrane arrangements are provided in the reaction chamber of the electrolyzer, which cause only the respectively desired gas, ie hydrogen and / or oxygen, to diffuse to the respective associated electrodes, while z. B.
- the residual gas is retained in the reaction chamber as a pure, dried carrier gas and can be withdrawn via a separate pipeline as a carrier gas line. At least part of this dried carrier gas can then be supplied to a liquid to be treated, in particular to a seawater and / or brackish water and / or wastewater or a waste liquid to be treated, as will be explained in more detail below.
- the gas accumulator designed as compressed gas storage is associated with a pressure regulating and / or alarm device which activates a blow-off device as a function of a predetermined overpressure via a discharge line, which preferably has a shut-off device and / or a non-return device.
- This blow-off device which is formed in particular by a blow-off valve, can be bridged by means of a bypass line in which a mechanical safety valve is arranged. With such a bypass line ensures that z. B. in the event of failure or failure of the pressure regulating and / or alarm device in any case a blow-off of the gas due to overpressure is possible.
- the mechanical safety valve can be z. B.
- an overpressure threshold be designed so that this responds later than the pressure regulating and / or alarm device associated electronic Abblasvoriques.
- a hydrogen storage as a gas storage is also associated with a safety torch to ensure that the escaping in the overpressure hydrogen gas can be safely flared.
- Another important advantage of the steam electrolysis of the present in vapor form in the carrier gas water is the fact that it is thus possible in principle to suck only the hydrogen gas and store, while the resulting oxygen is left in the carrier gas.
- the oxygen content in the carrier gas can be increased and used in the case of a desired wet combustion as the oxidant, so that no external oxygen supply is required.
- the resulting oxygen in addition to the hydrogen can also be sucked off and stored to this z. B. at predetermined times in predetermined amounts to feed the circuit, z. In the case of a desired wet combustion. Specifically, this z. B.
- an oxygen storage as gas storage an oxygen pipe to be assigned, preferably together with a shut-off device, preferably a shut-off valve, and / or a non-return, z. B. a check valve, via which by means of a control and / or regulating device at predetermined times, a predetermined amount of oxygen can be fed into the dried carrier gas stream.
- the oxygen pipeline is branched off from the gas storage pipeline and opens into a carrier gas line carrying the dried carrier gas stream.
- the To supply oxygen to other uses. So the oxygen z. B. be used for additional oxygen supply of biological wastewater treatment plants. The same applies in a figurative sense also to the steam-educt streams which are subjected to steam electrolysis.
- a liquid to be treated is distributed in the dried carrier gas stream and / or supplied from this to a predetermined number of treatment stations, in or in which the carrier gas stream is fractionated or successively from the solid and / or liquid contained in the liquid to be treated. or liquid and / or gaseous impurities and a hot water vapor carrier gas stream is provided.
- the treatment liquid is supplied to the mixing of the dried carrier gas for preheating and pre-cleaning at least one preheating-deposition, each having at least one preheating heat exchanger and a pre-heating heat exchanger downstream of the deposition device.
- the treatment liquid is preheated by the preheating heat exchanger to a temperature below the boiling temperature of the base liquid, so that evaporate with respect to the base liquid low impurities and / or the gaseous impurities are thermally expelled, wherein the evaporated and / or expelled impurities in the separator the at least one preheating separator are deposited.
- those low-boiling liquid impurities and / or gaseous impurities are separated from the treatment liquid, which can no longer be separated after the supply of the carrier gas.
- such a method and such a device can be used to process a very ready spectrum of a wide variety of treatment fluids with a multiplicity of different liquid and / or gaseous contaminants in an effective and economical manner.
- a process control and device in particular for the production of water, for.
- As in the form of drinking water or industrial water from sea and / or brackish water particularly well suited and advantageous because as part of the preheating and pre-cleaning the carbon dioxide dissolved therein in large quantities as well as the resulting in the thermal decomposition of HCO 3 carbon dioxide deposited and can be removed.
- the salts present in the base liquid can then be deposited in the course of evaporation of the base liquid as brine in the concentrate separator.
- the concentrate deposited in the concentrate separator is suitable as a hot water vapor starting material stream, which is fed to a water vapor electrolysis or a steam electrolyser, since the resulting concentrate stream has a relatively high liquid content which is necessary to ensure the flowability of the concentrate.
- the concentrate or the concentrate stream already has a temperature in the range of approx. 100 ° C to 150 0 C, drying by means of the steam electrolyzer can be performed very well in an energy-efficient manner. This procedure has the advantage that by means of a fractionated electrolysis a separation of recoverable salts or metals, ie of valuable substances, becomes possible.
- Another significant advantage of such steam electrolysis of the hot concentrate stream is that in the context of electrolysis, a heating takes place, which can be used in addition to the preheating of the liquid to be treated, preferably in conjunction with at least one concentrate / treatment liquid heat exchanger, before the admixture the treatment liquid to the dried carrier gas stream is flowed through by the treatment liquid for preheating.
- the residual drying of the concentrate stream up to a pourable mass can then z. B. in a thermal dryer, z. B. solar energy is used as a heat source.
- the piping and apparatuses can be dimensioned and dimensioned correspondingly smaller and less expensive. This is not least because already a part of the treatment liquid has been deducted as an impurity by the removal of the low-boiling liquid impurities before the supply of carrier gas.
- a carrier gas to be treated is supplied as a carrier gas, thus separating a fraction of the liquid impurities fractionated according to the boiling point temperature of the liquid impurities and / or an expulsion of the gaseous impurities from the resulting environmentally friendly disposal and Recycling recycled base liquid instead.
- the impurities can certainly also be valuable materials that can be recycled and do not have to be disposed of.
- a particularly advantageous efficiency of the system and of the process is achieved if the treatment liquid to be treated is fed in succession to at least two preheating separation devices connected in series.
- a particularly good and efficient separation effect is achieved with regard to the separation of the low-boiling impurities and / or the expulsion of the gaseous impurities.
- the conditioning liquid preheated in the at least one preheating heat exchanger of each preheating separation device is fed to an expansion device as part of the precipitation device, with which an effective separation of the low-boiling vaporous impurities and / or gaseous impurities takes place .
- the low-boiling vaporous impurities and / or the gaseous impurities can be fed from the expansion device via a line to a cooling device with heat exchanger as a further component of the separation device and stored in a collecting container so that a negative pressure is generated in the line during the cooling process, through which the separated impurities are sucked out of the expansion device.
- the expansion device can be formed by a decompression tank with an upstream pump or else by a pervaporation membrane system.
- each preheating heat exchanger is formed by a condensate-Beschsklongkeit- heat exchanger, with which a preheating is carried out by the hot, coming from the condensate tank condensate.
- a further heat input for the preheating of the treatment liquid in a concentrate-treatment liquid heat exchanger by the hot, coming from the steam electrolysis dried concentrate stream as Eduktstrom or, if such steam electrolysis for the concentrate stream should not be provided by the hot, coming from the concentrate collection concentrate take place, wherein the concentrate waste liquid heat exchanger of the at least one preheating-separating device is preferably connected upstream.
- the energy consumption can be significantly reduced overall, since almost all hot streams are used to heat colder streams. This also applies in particular when at least part of the heat supply for the evaporation to the wet carrier gas vapor mixture takes place in at least one evaporator condensation heat exchanger through the effluent, compressed and purified carrier gas dry steam mixture.
- the carrier gas is guided in a separate carrier gas circulation in order to minimize the carrier gas losses.
- a closed carrier gas circulation relatively expensive and valuable inert gases can be used as carrier gases due to the low carrier gas losses, which in their function as a carrier gas for the waste liquids against z. B. air are regularly preferred, since these are different than z. B. Air can not react with certain other components, in particular gaseous components of the waste liquids.
- additional gas drying may be provided behind a condensate header to dry wet residual carrier gas from the condensate header and to supply the carrier gas loop in the desired dry state.
- the resulting condensate in the condensate is discharged via a condensate drain line with a shut-off valve in a condensate collection container, wherein a possible carrier gas loss is achieved by a level measurement in conjunction with a control valve.
- the top product of the condensate collecting container which also has carrier gas constituents, is fed to an exhaust pipe connected on the top side of the condensate collecting vessel and then likewise fed to the carrier gas feed line via a heat exchanger as gas dryer with downstream condensate separator for carrier gas drying and via the gas line in a further carrier gas cycle.
- carrier gas can also be replenished in a simple manner via a coupled with the carrier gas circulation carrier gas storage.
- the supply takes place by a simple coupling in the existing carrier gas circulation, so that the system does not need to be stopped for this, which is uneconomical, but can be continuously operated.
- Another possible use in particular of the hydrogen obtained in the context of steam electrolysis is to accumulate the resulting gas in an internal combustion engine such.
- an internal combustion engine such as a gasoline engine to use at least one compressor of the processing plant to drive. If this internal combustion engine additionally connected to an electric generator, additional energy can also be obtained. This form of energy production and energy use causes a reduction in the primary energy demand and thus leads to a reduction of the CO 2 pollution of the atmosphere.
- air is provided as a carrier gas
- this can preferably be sucked from the environment, for. B. via a compressor which is provided with a suction filter.
- a corresponding flushing device z. B. at least one rinsing liquid container and / or at least one rinsing pump, by means of a rinsing medium, preferably a vorhaltenes in at least one rinsing liquid detergent, for flushing the pipes of the system can be pumped through this.
- the rinsing agent is preferably chosen so that it is adapted to the respective cleaning case, with basically several different rinsing agents can be kept ready.
- the flushing itself preferably takes place in a controlled or regulated manner according to a washing program predetermined by a control and / or regulating device for the respective cleaning case.
- a device or a method guide according to which or which at least one of the treatment fluids is particularly preferred umpumpende main pump at the same time in a dual function during the flushing process forms the flushing agent circulating flushing pump.
- the rinses themselves take place, for example, at predetermined intervals for and for given times, which depend on the particular concrete given rinse requirements.
- FIG. 1 is a schematic flow diagram of a device for the treatment of a liquid according to a first process, in which only hydrogen is split off in the context of steam electrolysis,
- FIG. 2 shows a schematic flow diagram of an apparatus for treating a liquid with an alternative process procedure, in which hydrogen and oxygen are split off as part of the steam electrolysis,
- FIG. 3 is a schematic flow diagram of a device for treating a liquid with an alternative process control, in which a control device is provided, with which a steam electrolyzer is charged with a predetermined amount of a hot water vapor carrier gas mixture, and
- FIG. 4 shows a schematic flow diagram of a device for treating a liquid with a further alternative process control, in which a fuel cell is provided.
- Treatment fluids such. B. incurred in production waste liquids, eg. As solvents in different dilutions, or sea and / or brackish water to be treated to drinking and service water are optionally pre-cleaned in a process control of FIG. 1 via an inlet 1 and by means of a pump 2 for preheating and pre-heating a preheating -Abborgetechnisch supplied having a preheating heat exchanger 7 and a pre-heating heat exchanger 7 downstream of the separator 14.
- the preheating heat exchanger 7 is formed here simultaneously as condensate-treatment liquid heat exchanger, which will be explained in more detail below, wherein in the preheating heat exchanger 7, the temperature of the treatment liquid to be purified is heated as close as possible to a desired evaporation temperature depending on the existing pressure.
- the separated steam and / or the separated gas are fed via a line 16 to a cooling device with heat exchanger 17 and stored in liquefied form in a collecting container 18.
- a negative pressure is created in the line 16 through which the discharge of the resulting gas and / or vapor from the separator 14 is effected.
- this can also be bridged via a bypass line 11 with corresponding shut-off devices 12 and 13.
- the supply line from the preheating heat exchanger 7 to the separator 14 is designated here by the reference numeral 9.
- a shut-off device 10 is also provided.
- the z. B. designed as a flash tank separator 14 is further associated with a pump 21, which together form a relaxation device.
- the preheated and prepurified treatment liquid is then passed via a pipe 22 to a mixing device 8, which is further connected to a carrier gas line 63, and in the finest distribution of the preheated and prepurified treatment liquid in the supplied by the carrier gas line 63 dried carrier gas stream.
- a mixture line 25 this resulting wet carrier gas vapor mixture is passed into an evaporator / condensation heat exchanger 27, in which further heating takes place with the aim of overheating the carrier gas vapor mixture.
- the required temperatures and operating pressures of the carrier gas vapor mixture are dependent on the components to be separated and the thermal parameters of the waste liquid to be cleaned. Therefore, temperatures between 50 and 25O 0 C and operating pressures between 0.5 bar and 20 bar may be required.
- the wet carrier gas vapor mixture with the liquid residue which has a higher boiling point with respect to the base liquid and the treatment liquid to be purified in the base liquid is subsequently introduced by means of a pipe into a concentrate separator 30, in which this liquid residue and / or a brine as concentrate is deposited.
- This Konzentratabscheider 30 may be formed, for example, as a cyclone or baffle plate. In the case of the baffle plate separator, both single-plate and multi-plate separators can be used.
- the carrier gas / dry steam mixture now containing no residual liquid leaves the concentrate separator 30 via a line 31 and is fed to a droplet separator 32, in which concentrate still contained in the carrier gas / dry steam mixture can be separated and fed to a concentrate receiver 97 via a pipeline 98.
- the concentrate collected in the concentrate collection container 97 is discharged via a pipe 99, wherein the hot concentrate may optionally serve for preheating the waste liquid 1 supplied to the preheating heat exchanger 7, which is not shown here.
- the droplet separator 32 leaving the carrier gas dry steam mixture is supplied via a pipe 33 to a compressor 36, whereby the carrier gas dry steam mixture is brought to the desired operating pressure with simultaneous increase in temperature.
- This compressed carrier gas-dry vapor mixture passes through a pressure line 37 in the evaporator / condensation heat exchanger 27 and is there under condensation of the dry steam of the carrier gas dry steam mixture, namely the base liquid of the treatment liquid, cooled, at the same time heating the wet carrier gas vapor mixture, the the interference of the dried carrier gas stream comes, takes place.
- the mixture coming from the evaporator / condensation heat exchanger 27 is then passed via a pipeline 41 to a condensate separator 43, in which the condensate is separated.
- condensate 43 comes here z.
- the accumulating in the condensate 43 condensate is collected in a condensate tank 44 and passes through a pipe 45 into a separator 48, where any medium boilers such.
- H 4 N 2 , CI 3 N, H 2 O 2 , CCI 3 NO 2 are deposited in conjunction with a cooling device 50 and a collecting container 51, so that the now formed by a high purity base liquid condensate through a pipe 52 for preheating Heat exchanger 7 is guided, it after the heat exchange with the treatment liquid via a pipe 54 as z. B. leaving the process water.
- the hot, laden with non-condensed water vapor carrier gas passes after the Kondensatabscheider 43 as a hot water vapor carrier gas stream via a Absperrvorrich- device 57 in a reaction space of a hydrogen electrolyzer 58, in which at least one anode 60 and at least one cathode 59 are arranged. These electrodes 59, 60 are supplied with electrical energy by means of a rectifier 62.
- the cathode 59 is separated by means of an ion-specific membrane from the reaction space through which the resulting hydrogen gas can diffuse through, the residual gas, however, not.
- the extraction takes place via a pipeline 69, in which a shut-off device 70 and a non-return valve 71 are arranged, by means of a vacuum pump 72.
- a pressure line 73 in which a non-return valve 75 and a shut-off device 76 are arranged, the hydrogen gas in promoted a compressed gas storage 77.
- a pressure regulating and alarm device 78 is mounted for monitoring and securing, is controlled by the regulated via a line 79 with a check valve 80 and a non-return valve 81, a possible overpressure by means of an automatic blow-off valve 82.
- a bypass line 84 is provided with a mechanical safety valve 85.
- the effluent hydrogen gas is burned harmless by means of the safety torch 83.
- the after-dried carrier gas returns from the electrolyzer 58, via the line 63, back to the carrier gas circuit with a flow rate measuring device 65 and a pressure and temperature measuring device 64 coupled to a control valve 67.
- an emergency relief in connection with the pressure line 37 is provided via the lines 105, 106 with safety valves 107, 108 arranged therein, but will not be discussed in more detail here.
- a switchable by means of shut-off devices 103 and 104 pressure line 102 is provided, via which a purge for the pressure line 37 via the pipe 99 is possible.
- z. B. be sucked in the case of air as the carrier gas via a compressor 86 with suction air from the environment and be fed via an air line 88 in the carrier gas circulation, z. B. for starting the device or for refilling of carrier gas.
- an injection of air as a sealing gas for the shaft seals of the compression chamber of the compressor 36 via the air lines 92, 94 with the interposition of a collecting container 93 in the region of the compressor 36 done.
- FIG. 2 shows a schematic flow diagram of an alternative device, which differs from the device according to FIG. 1 only by the separation of both hydrogen gas and oxygen gas, so that reference will be made hereinafter only and with respect to the remainder of the process of the structure to the previously made statements to Fig. 1 is referenced.
- the hot, laden with non-condensed water vapor carrier gas thus passes here after the condensate 43 via a shut-off device 57 in a reaction space of the hydrogen electrolyzer 58, in turn, an anode 60 and cathode 59 are arranged as electrodes, by means of a rectifier 163 with the necessary electrical energy to be supplied.
- Both the cathode 59 and the anode 60 are separated by means of ion-specific membrane from the reaction space, through which the respective resulting hydrogen gas or the respective resulting oxygen gas can diffuse through, the residual gas, d. H. the pure carrier gas is not.
- effluent hydrogen gas is burned harmless 177 by means of a safety torch.
- the resulting oxygen gas is supplied by means of a vacuum pump 183 via a suction line
- a pressure relief device consisting of a discharge line 190 with a non-return valve 192 and a shut-off device 191 and a controllable blow-off valve 193 is arranged.
- the blow-off line 190 has a bypass 194 with a mechanical safety valve 195.
- the oxygen pressure line 184 is connected by means of a pressure line 196, in which a non-return valve 197 and a shut-off 198 are connected to a carrier gas line 199, so that a partial return of oxygen in the carrier circuit can be carried out according to the respective requirements, if this according to the respective task should be required.
- the after-dried carrier gas returns from the electrolyzer 58 via the carrier gas line 199 with a flow rate measuring device 100 and a pressure and temperature measuring device 101 back into the carrier gas cycle.
- FIG. 3 shows a schematic flow diagram representation of a further variant of the invention in which, again, essential components of the system correspond identically to those of the embodiments of FIGS. 1 and 2, so that reference is made to the relevant embodiments of FIG.
- only a portion of the hot steam-laden steam can be used in accordance with the requirements for the degree of drying of the dry carrier gas stream or depending on the need for hydrogen.
- Charge carrier gas to be fed to a steam electrolyser to be fed to a steam electrolyser.
- the selected subset of hot, wet steam-carrier gas mixture is guided by means of a quantity measuring device 263 in a supply line 262 to the electrolysis cell or to the electrolyzer 265, wherein the preselected amount is adjusted by means of the flow rate measuring device 263 via a control valve 264.
- a quantity measuring device 263 in a supply line 262 to the electrolysis cell or to the electrolyzer 265, wherein the preselected amount is adjusted by means of the flow rate measuring device 263 via a control valve 264.
- at least one anode 267 and a cathode 266 are arranged. These electrodes 266, 267 are supplied with electrical energy by means of a rectifier 269.
- the cathode 266 is separated by an ion-specific membrane from the reaction space through which the resulting hydrogen gas can diffuse through, the residual gas, however, not.
- the suction takes place here via a pipe 272, in which a shut-off device 273 and a non-return 274 are arranged, by means of a vacuum pump 275.
- a pressure line 276, in which a non-return valve 278 and a shut-off device 279 are arranged the hydrogen gas in a Compressed gas storage 280 promoted.
- a pressure regulating and alarm device 281 is mounted for monitoring and securing, through which, via a line 282 with a shut-off valve 283 and a non-return valve 284, a possible overpressure by means of an automatic blow-off valve 285 can be drained.
- a bypass line 286 with a mechanical safety valve 287 in the manner previously described in connection with FIG. 1 is also provided here.
- the effluent hydrogen gas can be flared harmlessly by means of a safety torch 283.
- the after-dried carrier gas returns from the electrolyzer 265 via a line 270 with a flow rate measuring device 250 and a pressure and temperature measuring device 249 back into the carrier gas circulation via a line 248.
- Via this line 248 we are also the optionally not introduced into the electrolyzer 265 partial flow of the hot water vapor carrier gas stream in the carrier gas circulation in the previously described manner returned.
- the content of hydrogen in the dried carrier gas stream can be measured by means of a measuring device 271, which includes a feedback to the control valve 264 including flow rate measurement via the quantity measuring device 263.
- FIG. 3 has been described here analogously to FIG. 1 with only the elimination of hydrogen.
- this variant can also be used in conjunction with an embodiment according to FIG. 2, according to which both hydrogen gas and oxygen gas are split off during the electrolysis.
- 4 shows a further alternative process control and embodiment of the device according to the invention for processing a liquid, in particular a waste liquid, which is based essentially on the process control according to the schematic flow diagram of FIG. 2, in which a compressed gas reservoir 171 for the hydrogen gas and a compressed gas storage 188 is provided for the oxygen gas.
- a compressed gas reservoir 171 for the hydrogen gas and a compressed gas storage 188 is provided for the oxygen gas.
- a predetermined amount of hydrogen gas or oxygen gas is taken from the two compressed gas reservoirs 171, 188 and a fuel cell 303 at predetermined times by means of a valve device 301, 302, which are respectively controlled according to predetermined operating parameters by a control and regulating device fed.
- a valve device 301, 302 which are respectively controlled according to predetermined operating parameters by a control and regulating device fed.
- electrical energy can then be generated, which in turn can be supplied to selected electrical consumers of the treatment plant according to the invention, as will be explained in more detail below.
- the hot concentrate flowing from the concentrate collection container 97 is piped to another steam electrolyser 304 fed, in the example shown here, the entire concentrate stream, but only the supply of a partial flow is possible.
- the steam electrolyser 304 is substantially identical to the steam electrolyser 58 and also has at least one cathode 305 and at least one anode 306. With regard to the further construction and the mode of operation, reference is made here, in order to avoid repetition, to the description of the steam electrolyser 58, which applies analogously here.
- the hydrogen gas or oxygen gas produced in the steam electrolyzer 304 is applied via z. B. vacuum pumps 307, 308 deducted from the steam electrolyser 304 and stored in the respective associated compressed gas storage 171 for the hydrogen gas and 188 for the oxygen gas.
- the dried concentrate stream 309 leaving the steam electrolyzer 304 is then fed to a concentrate / treatment liquid heat exchanger 310 which is further flowed through by the treatment liquid 1, the hot concentrate stream 309 giving heat to the waste liquid 1 and further preheating it.
- the thus preheated treatment liquid 1 is supplied to a pump reservoir 311, from which then the treatment liquid can be withdrawn in the preheated state by means of the pump 2 in the manner described above.
- the concentrate stream 312 cooled in the concentrate / treatment liquid heat exchanger 310 is then fed to a solar-powered thermal dryer 312, where the residual drying takes place and z.
- a solar-powered thermal dryer 312 As salts or metals can be obtained as recyclables.
- the power supply of the steam electrolyzers 58 and 304 may be at least in part by means of the electrical energy supplied by the fuel cell 303.
- two compressors 36 are additionally provided here, to which partial streams of the carrier gas dry steam mixture leaving the droplet separator 32 are supplied via the pipeline 33.
- the compressor 36 which is also referred to as a booster, the carrier gas dry steam mixture, as described above, is brought to the desired operating pressure with a simultaneous increase in temperature.
- the use of two compressors 36 substantially increases the throughput through this compression station.
- a compressor 36 in operation d. h., That the second compressor is turned off and can be optionally switched on if necessary.
- more than two compressors can be used, but this is not explicitly described here.
- a cooling circuit 316 For cooling the two compressors 36, a cooling circuit 316 is provided which comprises two pumps 317, 318 which pump cooling liquid, preferably water from a reservoir 320 as a pump reservoir to the two compressors 36, where the cooling liquid cools the compressors 36 and then subsequently in the preheated Condition is passed through a cooling liquid / treatment liquid heat exchanger 319, on the other hand, is also flowed through by the treatment liquid 1, so that the treatment liquid 1 is also preheated by this measure.
- the oil in the compressors 36 is substantially cooled to prevent diffusion of oil vapors into the compression space and to maintain the lubricity.
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- Chemical & Material Sciences (AREA)
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- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Metallurgy (AREA)
- Materials Engineering (AREA)
- Electrochemistry (AREA)
- Hydrology & Water Resources (AREA)
- Inorganic Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
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Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE200710017613 DE102007017613A1 (en) | 2007-04-12 | 2007-04-12 | Method and device for the treatment of liquids |
PCT/EP2008/002864 WO2008125283A1 (en) | 2007-04-12 | 2008-04-11 | Method and device for treating liquids, using an electrolytic drying stage |
Publications (1)
Publication Number | Publication Date |
---|---|
EP2134434A1 true EP2134434A1 (en) | 2009-12-23 |
Family
ID=39735168
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP08735170A Withdrawn EP2134434A1 (en) | 2007-04-12 | 2008-04-11 | Method and device for treating liquids, using an electrolytic drying stage |
Country Status (6)
Country | Link |
---|---|
US (1) | US8747648B2 (en) |
EP (1) | EP2134434A1 (en) |
BR (1) | BRPI0809793A2 (en) |
DE (1) | DE102007017613A1 (en) |
WO (1) | WO2008125283A1 (en) |
ZA (1) | ZA200906966B (en) |
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US20100154429A1 (en) * | 2008-11-24 | 2010-06-24 | Peters Bruce H | Water Purification |
US20100126876A1 (en) * | 2008-11-24 | 2010-05-27 | Peters Bruce H | Water Purification |
US20100224477A1 (en) * | 2009-03-09 | 2010-09-09 | Peters Bruce H | Water Purification |
DE102009012668A1 (en) * | 2009-03-13 | 2010-09-16 | E.On Anlagenservice Gmbh | Process and plant for the utilization of biomass |
EP2507410B1 (en) * | 2009-12-01 | 2017-11-01 | Neubert, Susanne | Process and apparatus for producing hydrogen by means of electrolysis |
EP2377972B1 (en) * | 2010-04-19 | 2014-03-05 | GP Joule Holding GmbH & Co. KG | Device for electric generation of hydrogen |
US20110281959A1 (en) * | 2010-05-11 | 2011-11-17 | The Government Of The United States Of America As Represented By The Secretary Of The Navy | Extraction of Carbon Dioxide and Hydrogen From Seawater and Hydrocarbon Production Therefrom |
WO2012128984A2 (en) * | 2011-03-23 | 2012-09-27 | Smartpool, Inc. | Heating system with integrated hydrogen generation |
US8721980B2 (en) | 2011-03-30 | 2014-05-13 | Altmerge, Llc | Systems and methods of producing chemical compounds |
US9187335B2 (en) | 2011-03-30 | 2015-11-17 | Altmerge, Llc | Pulse jet water desalination and purification |
WO2012134521A1 (en) | 2011-03-30 | 2012-10-04 | Altmerge, Llc | Systems and methods of producing chemical compounds |
US10343118B2 (en) * | 2011-12-22 | 2019-07-09 | Water Standard Company (Mi) | Method and control devices for production of consistent water quality from membrane-based water treatment for use in improved hydrocarbon recovery operations |
US10329171B2 (en) | 2011-12-22 | 2019-06-25 | Water Standard Company (Mi) | Method and control devices for production of consistent water quality from membrane-based water treatment for use in improved hydrocarbon recovery operations |
CN102786174B (en) * | 2012-03-29 | 2013-12-18 | 波鹰(厦门)科技有限公司 | Seawater desalination device and method thereof |
CN103290633B (en) * | 2013-05-31 | 2015-01-21 | 浙江斯帝特新能源有限公司 | Solar dyeing machine system with function of gradient use of heat |
CN103800979B (en) * | 2013-06-19 | 2018-05-04 | 林信涌 | Health care gas generator |
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JP6636790B2 (en) * | 2015-12-18 | 2020-01-29 | 株式会社東芝 | Hydrogen peroxide generator |
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KR20180066578A (en) * | 2016-12-09 | 2018-06-19 | 엘지전자 주식회사 | Drinking water supplying device and Controlling method for the same |
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CN111068471A (en) * | 2019-11-27 | 2020-04-28 | 云南电网有限责任公司电力科学研究院 | Device for preparing dry air on site |
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CN111870975A (en) * | 2020-06-11 | 2020-11-03 | 岳玉亮 | Solution concentration device for heat source tower system |
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2008
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- 2008-04-11 BR BRPI0809793 patent/BRPI0809793A2/en not_active IP Right Cessation
- 2008-04-11 WO PCT/EP2008/002864 patent/WO2008125283A1/en active Application Filing
- 2008-04-11 US US12/450,785 patent/US8747648B2/en active Active
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2009
- 2009-10-07 ZA ZA200906966A patent/ZA200906966B/en unknown
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Also Published As
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WO2008125283A1 (en) | 2008-10-23 |
BRPI0809793A2 (en) | 2014-10-07 |
US20100187128A1 (en) | 2010-07-29 |
DE102007017613A1 (en) | 2008-10-23 |
US8747648B2 (en) | 2014-06-10 |
ZA200906966B (en) | 2010-05-26 |
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