WO2000041462A2 - Process and apparatus for cleaning of waste water - Google Patents
Process and apparatus for cleaning of waste water Download PDFInfo
- Publication number
- WO2000041462A2 WO2000041462A2 PCT/DK2000/000013 DK0000013W WO0041462A2 WO 2000041462 A2 WO2000041462 A2 WO 2000041462A2 DK 0000013 W DK0000013 W DK 0000013W WO 0041462 A2 WO0041462 A2 WO 0041462A2
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- WO
- WIPO (PCT)
- Prior art keywords
- compounds
- column
- heat exchanger
- steam
- liquid
- Prior art date
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Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- 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
- B01D5/0075—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with heat exchanging
-
- 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
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/009—Collecting, removing and/or treatment of the condensate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- 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
- C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
Definitions
- the present invention relates to a process for improving plants for waste water cleaning, in which evaporation by means of steam compression as a cleaning method is a part.
- Waste water cleaning plants which use evaporation by means of steam compression, are typically minor plants for cleaning of a special kind of waste water such as e.g. heavy metal containing waste water, used cooling lubricants, water-based degrease liquids and waste water from various washing processes.
- the cleaned water has hitherto typically been reused or drained off for canalization.
- Types of waste water containing big amounts of compounds which are mobile at the temperature and the pH at which the evaporation is taking place, are normally not suited for a cleaning-up process in a waste water cleaning plant, which uses evaporation by means of steam com- pression, because the cleaned water as a rule will be too unclean for re-use, and furthermore a draining off for canalization will be very problematic, because of a too big remaining content of mobile compound.
- the process described in this invention makes waste water cleaning plants with evapo- ration by means of steam compression especially suited for cleaning of biological waste water containing mobile compounds in form of weak acids and weak bases.
- waste water which often contains big amounts of mobile compounds
- waste water which is produced in connection with one or more biological processes, such as e.g. manure from pigs, manure from catties, toilet water, waste water from production of medicamentn, washing water from slaughteries and cooling lubricants, including said kinds of waste water, which have putrefied.
- biological processes such as e.g. manure from pigs, manure from catties, toilet water, waste water from production of medicamentn, washing water from slaughteries and cooling lubricants, including said kinds of waste water, which have putrefied.
- a big part of the mobile compounds, which normally evolve by biological decomposition processes will be present as weak acid/base couples.
- the present invention relates to a process for cleaning of biological waste water, which contains more mobile compounds and less mobile compounds in relation to the mobility of water, and which are present as weak acids and weak basis.
- the proces uses inter alia an evaporation of the waste water, where the waste water is heated in a boiler.
- the formed steam is cleaned by this approach for unwanted gaseous compounds, and it is transferred from this boiling step via a compression step to a heat exchanging step, where the water is condensed and drained off in cleaned form to the recipient, and where the bigger part of the more mobile compounds is concentrated and drained off together with the remaining fraction of steam.
- the invention encompasses furthermore an apparatus for the embodiment of the proc- ess.
- these more mobile compounds consist of compounds which are not condensable by the magnitudes of pressure and temperature which are applied by the evaporation of the basic liquid of the solution, which normally is water, and therefore they will be inhibitory for the evaporation of water, because they are present as an insulating layer within the heat exchanger. Because such a layer will act as an inhibitor for the heat transmission to the condensable compounds within the heat ex- changer it will implicate an increase of the energy consumption.
- Another main compound which belongs to the group of the more compounds, is frequently as mentioned above ammonia, which it is likewise desirable to remove, before the vapours are led into the heat exchanger.
- An applicable method for this is to con- duct the ammonia vapours through a scrubber, as it is described in patent DK 17161 1.
- the present invention comprises furthermore a removal of these compounds.
- a method for this is described in patent application DK 01288/96, according to which a concentration of the compounds firstly takes place in the boiler used for the above described evaporation.
- the heated liquid is being led to a column, from which the more mobile compounds in gaseous form are led to the primary side of a first heat exchanger, so that these more mobile compounds are condensed and led out from the primary side, and from the same column the less mobile compounds are led in liquid form to the secondary side of the above mentioned first heat exchanger, where they are heat exchanged with the condensed more mobile compounds.
- the present method is remarkable by a decreased enery consumption in relation to known methods and a consumption of chemicals which is totally eliminated.
- the invention will as an example in the following be described in more detail based on cleaning of manure, the method, however, is not to be limited to this.
- Examples of other liquids, which can be cleaned by an approach according to the present invention are - apart from the above mentioned biological waste liquids in general, which as already known inter alia comprise manure - emulgated liquids, as e.g. cooling/oil lubricants oil emulsions, degreasing liquids, oil containing waste water, waste water from laundries, solvents and waste water from food production and its like.
- the unwanted compound will comprise CO 2 , NH 3 , NH 4 + , fatty acids, including CH 3 COOH, and other organic liquids.
- the unwanted compounds can be present in neutral and/or charged form and/or as salts.
- a method and an apparatus of the known type can as an example be formed according to the disclosure in patent DK 171611. Here manure is de-gassed and during subsequent passage through a scrubber the present ammonia and acetic acid are neutralized by addition of calculated amount of acid and base.
- Fig. 1 shows a plant for waste water cleaning with known technology by means of the scrubber 52 (comprising scrubber 53 and scrubber 54),
- Fig. 2 shows a diagramme of an embodiment of a scrubber with known technology
- Fig. 3 shows a diagramme of an embodiment of the technology in a plant, which uses the present invention with column and heat exchanger,
- Fig. 4 shows especially that part of the plant with combination of a column and a heat exchanger in Fig. 3, which the present invention makes use of,
- Fig. 5 shows in- and outlets from a column in an embodiment according to the pre- sent invention and the relevant chemical equilibriums
- Fig. 6 shows a diagramme of an embodiment of a heat exchanger with its in- and outlets according to the present invention.
- Fig. 1 shows a schematic illustration of an example of an embodiment for a plant according to known technology from Danish patent application DK 01288/96.
- the plant comprises a column 1, a first heat exchanger 2, a compressor 3, a bottom vessel 4 for the column 1, a circulation pump 5 receiving liquid from outlet 36, a motor valve 6, a contravalve 7, a gas/liquid separator 8, a level sensor 9 for control of liquid level in the bottom vessel 4 for column 1, a first section 10 of a second heat exchanger, a second section 11 of the second heat exchanger, a third heat exchanger 12, a first motor valve 13, and a second motor valve 14.
- the column 1 is provided with nozzles 15 for draining off of liquid biological waste in column 1.
- the column 1 is provided with an inlet 16 for the liquid biological waste to the column 1.
- liquid biological waste will as mentioned manure be applied in the following part of the description.
- the manure is led to the column 1 in order to be separated in column 1 into more mobile compounds and less mobile compounds.
- the more mobile compounds are led to a foam restrictor 17 in an upper part of the column 1.
- the less mobile compounds are led to the bottom vessel 4 in the bottom of column 1.
- the more mobile compounds will inter alia comprise carbon dioxide (CO 2 ) and ammonia (NH 3 ), and the less mobile compounds will inter alia comprise water (H 2 O), fatty acids and mineral salts.
- the manure Before the manure is led to column 1 the manure is heated, because it is led through a secondary side of the first section 10 and a secondary side of the second section 1 1 of the second heat exchanger.
- the first section 10 of the second heat exchanger is provided with an inlet 18 for the manure.
- the inlet 18 is provided with a motor valve 14 for inlet of the manure to the first section 10.
- the first section 10 is provided with an outlet 19, which leads to an inlet 20 for the second section 1 1 of the second heat exchanger.
- the second section 11 is provided with an outlet 21 , which leads to the inlet 16 to the column 1.
- the manure is supposed to achieve a rise of temperature to the boiling point of the manure, before the manure is led to the nozzles 15 in column 1.
- the more mobile compounds are led from an outlet 22 from the foam restrictor 17 to the compressor 3, where the more mobile compounds are compressed.
- the more mobile compounds are led to an inlet 23 of a primary side of the first heat exchanger 2.
- the more mobile compounds are led through the primary side of the first heat exchanger 2 to an outlet 24 from the primary side of the first heat exchanger 2.
- the more mobile compounds are thereafter led to an inlet 25 of a primary side of the second section 11 of the second heat exchanger.
- the more mobile compounds are led through the primary side of the second section 11 and to an outlet 26 of the second section 11 of a second heat exchanger.
- the more mobile compounds After being led through the primary side of the first heat exchanger 2, respectively the second section 1 1 of th second heat exchanger the more mobile compounds are partly condensed and consist of a gas fraction and a liquid fraction. From the outlet 26 of the primary side of the second section of the second heat exchanger the gas fraction and the liquid fraction of the more mobile compounds are led to an inlet 27 to the gas/liquid separator 8.
- the liquid fraction from an outlet 28 of the separator 8 is led to an inlet 29 of the liquid fraction and to nozzles 30 in column 1 as reflux.
- the gas fraction from the separa- tor 8 with the more mobile compounds are from an outlet 31 led to an inlet 32 to a primary side of the third heat exchanger 12.
- a total condensing of the gas fraction is taking place.
- the carbon dioxide (CO 2 ) diffuses into the liquid, where it together with water (H 2 O) and ammonia (NH 3 ) form ammonia hydrogen carbonate (NH 4 HCO 3 ).
- This ammonia hy- drogen carbonate is led to an outlet 33 from the primary side of the third heat exchanger and it can be stored in a normal closed container (not shown) and can be drained off from here.
- Those parts of the manure, which are led to the second heat exchanger, are as a start led to a secondary side of the third heat exchanger 12.
- the manure is led to an inlet 34 to the secondary side of the third heat exchanger 12 by means of the first motor valve 13 and through the secondary side of the third heat exchanger 12 to an outlet 35 from the secondary side. From the outlet 35 of the secondary side of the third heat exchanger 12 the manure is led through the inlet 20 of the secondary side of the second section 11 of the second heat exchanger.
- the draining off from the secondary side of first heat exchanger 2 is taking place through outlet 38, through the contra valve 7 and the motor valve 6.
- the part of the liquid containing the less mobile compounds can be described as de-gassed, this is to say free of the more mobile compounds, and it can be led further on to a possible additional treatment such as an evaporation.
- the more mobile compounds will by compression in the compressor 3 achieve a temperature which is higher than the temperature of the manure being led to the nozzles 15 of the column 1.
- the less mobile compounds are led following passage of the motor valve 6 to a vessel 41 for the processing, which is connected with the scrubber 52 (comprising scrubber 53 and scrubber 54), and the functional correlation can be formed as described in patent application DK 0868/94, and reference is made to the following Fig. 2.
- the polluted liquid is heated in the vessel 41 for the processing linked to the scrubber 52 (comprising the scrubber 53 and the scrubber 54), whereafter a circulation pump 43 (connected with outlet from the processing vessel) is conducting the liquid to the top of the evaporator.
- an outlet is provided, which can drain off the concentrated and polluted part of from the processing vessel 41, which is linked to the scrubber 52 (comprising the scrubber 53 and the scrubber 54.
- a steam tapping 47 is provided, which is linked to a compressor 49, which furthermore via said scrubber 52 is connected with a downdraught evaporation heat exchanger 50, which is placed above the container for the processing vessel 41 (linked to the scrubber 52) within the evaporator.
- an outlet pipe 51 is placed for the clean condensate.
- Fig. 2 shows a plant of known type from Danish patent application DK 0868/94 comprising inter alia an evaporator 39 and the scrubber 52.
- a liquid distribution system 40 is provided, and at the bottom the vessel for the process- ing 41 is present (linked with the scrubber 52), which contains the concentrated processing liquid 42 (abbreviated C c ).
- the vessel for the processing 41 is connected with a circulation pump 43 and a circulation pipe 44, which pumps the heated and polluted processing liquid 42 to the distribution system 40 at the top of the evaporator.
- the vessel 41 for the processing which as mentioned is connected to the scrubber 52, has an inlet pipe 45 for supply of polluted processing liquid 42 and an outlet pipe 46, which is used for emptying of the concentrated and polluting concentrate (abbreviated C c ) from the vessel 41 for the processing, which is connected to the scrubber 52 (comprising the scrubber 53 and the scrubber 54).
- C c concentrated and polluting concentrate
- a steam tapping 47 is provided, which via a pipeline 48 and a compressor 49 is connected with a downdraught evaporation heat exchanger 50, which is placed inside the evaporator 39.
- a downdraught evaporation heat exchanger 50 which is placed inside the evaporator 39.
- an outlet 51 is provided for clean condensate.
- the scrubber 52 (comprising the scrubber 53 and the scrubber 54) is placed in the steam pipe 48, in which also the compressor 49 is mounted. In the shown situation the scrubber 52 is placed upstream to the compressor 49. This is preferred, but it is also without difficulty possible to place the scrubber 52 downstream to the compressor 49.
- the polluted and concentrated process liquid 42 is transferred batchwise at the pipe 45 and drained off after an concentration has taken place via the outlet pipe 46.
- the clean condensate is drained off via the outlet pipe 51.
- the scrubber 52 comprises a first and a second scrubbing step 53, 54.
- the scrubber 53 contains an acid 55
- the scrubber 54 contains a base 56.
- Each of the scrubbers 53, 54 is provided with a pipe for acid 57 and a pipe for base 58.
- the shown level 60 for the processing liquid is achieved at a certain point of time, after which a float switch for regulation of the inlet of the polluted liquid 61 is activated, whereby a heating element (not shown) and a circulation pump 43 are switched on.
- the temperature is hereby increased to a temperature and pressure, which is closely below the boiling point of the liquid, which is to be cleaned (the condensate). If the liquid is water the temperature is increased to approximately 100°C.
- the circulation pump 43 is started up in the plant to ensure that all components have the same temperature.
- the compressor 49 is started.
- the compressur 49 creates a vacuum in the processing vessel 41 linked to the scrubber 52 and thereby forces the steam placed over the polluted and concentrated processing liquid 42 through the scrubber 42, after which the steam via the pipeline 48 is transferred to the heat exchanger 50, where heat exchange is taking place of the steam at the one side of the heat exchanger and the heated, polluted and concentrated processing liquid 42 on the second side of the heat exchanger.
- the steam which has been compressed in the compressor 49, will loose its energy, which is transferred to the circulated polluted liquid 42 on the second side of the heat exchanger.
- a scrubber 52 Within the pipe from the compressor 49 to the downdraught evaporation heat ex- changer 50 a scrubber 52 has been placed, which as mentioned above is separated into two parts.
- the upper part 54 contains a base (NaOH) and the lower part 53 an acid (HNO 3 ), which are supplied through a pipe for each liquid.
- the upperstream part in the scrubber 52 (comprising the scrubber 53 and the scrubber 54) must always be supplied with acid in relation to the downstream alkaline part, because the acids are more mobile than the bases.
- Both parts in the scrubber 52 are provided with devices for inhibition of bubbles, ripples and its like, which promotes splash and thereby risk of bringing droplets out into the steam pipe from the scrubber 52 to the heat exchanger 50.
- the present approach which is disclosed by this invention, is new and is remarkable in a surprising way which is advantageous in relation to the prior art and knowledge, including especially DK patent application 01288/96.
- the process according to the invention makes use of a mechanic and a process technical construction, which is more simple than the hitherto known technique within this field, which gives a lower level of expenditures. Apart from this the embodiment of this process renders advantages. It is thus a remarkable feature that the process is carried without supply and use of chemicals, which is a new and an obvious advantage with regard to the time period within which the process is taking place, as well as outside this time period. Concern- ing the time period in which the process is taking place, the hitherto known technology required thus a handling of the supply of the chemicals needed for the process.
- the process according to the invention also has that economic advantage that the expenditures for purchase of chemicals are avoided, which makes the embodiment of the process cheaper in relation to the closest known technique.
- the disadvantages by the known technology, which is here shown by an example of a plant, is thus clearly that the operation is connected with the relatively high consumption of energy and a high use of chemicals.
- Fig. 3 shows an example of a flowsheet for a plant, which uses this invention.
- the apparatus which is shown in Fig. 3, consists of a downdraught evaporation heat exchanger 50, through which the liquid, that is under evaporation and is to be cleaned, is circulated by means of the circulation pump 43, connected with the outlet from the processing vessel.
- the boiler liquid 42 is heat exchanging on its way down through the heat exchanger 50 with the condensing water steam from a absorption column 62, which constitutes an essential part of the present invention.
- acid/base reactions are taking place as something very essential for the invention.
- Said acid/base reactions are taking place between the present weak acids and weak bases, which as mentioned are more mobile compounds and less mobile compounds as judged relatively to the mobility of water.
- the heat exchanging 50 the liquid is brought to the boiling point.
- the downdraught evaporation heat exchanger 50 is placed above the boiler 42 in which a reservoir of liquid being under evaporation is present.
- the liquid is circulated by means of the pump 43.
- the pressure in the boiler 42 is kept constant during the evaporation by means of a pressor state 63 (for regulation of the heating element 64) which is activated when the pressure is below 5 mmbar overpressure compared to the surroundings.
- the steam which arises by the boiling of the liquid in the heat exchanger 50 is streaming together with the liquid down into the boiler 42.
- a liquid/steam separator 65 is placed which separates liquid and steam from each other, whereby the liquid is kept within the boiler 42, which the steam leaves through the separator 65.
- the steam flows from the liquid/steam separator 65 to the absorption column 62, in which the main part of impurities in the steam is removed. From the abso ⁇ tion column 62 the steam is flowing to the compressor 49, which gives the steam an increase pressure, whereby the condensation temperature of the steam increases to such a degree that the steam is able to condense, when it flows over to the heat exchanger 50.
- the condensate from the steam runs down to the bottom of the heat exchanger 50, in which it is collected until a certain level is achieved, which is determined by the float switch 66, which by activation opens valve 67 which permits the condensate to flow to the vessel 68.
- valve 70 which opens by activation through the float switch 69 which permits that the liquid which is to evaporate flows through said valve 70, a first heat exchanger 71 (in which the polluted liquid heat exchanges with the condensate), a second preheat exchanger 72 (in which the polluted liquid is heat exchanging with the steam) and is mixed with the liquid from the boiler 42, which is under evaporation and thereafter introduced into the downdraught evaporation heat exchanger 50.
- first heat exchanger 71 in which the polluted liquid heat exchanges with the condensate
- second preheat exchanger 72 in which the polluted liquid is heat exchanging with the steam
- a reservoir of condensate is collected until the level which is determined by the level sensor 73 is achieved, which permits that the valve 74 opens and 75-95% of the condensate (abbreviated C d ) leaves the apparatus through the first preheat exchanger 71, which is the heat exchanger which receives the incoming aque- ous liquid W.
- a part of the condensate (5%-25%) is pumped by means of pump 75 to the top of the abso ⁇ tion column 62, in which it is distributed to the column elements within the column.
- the condensate absorbs the im- purities from the steam, which rises up from the boiler 42 and acid/base reactions are taking place. In the legend to Fig. 4 these reactions are further explained.
- the condensate containing the impurities is led from the bottom of the abso ⁇ tion column 62 to the process vessel 41, which is connected to the scrubber 52, in which it is mixed with the liquid which is under evaporation and cleaning.
- the part of the steam containing the more mobile compounds is led from the column 62 via the compressor 49 to the heat exchanger 50.
- the part hereof, which by passing through the heat ex- changer 50, is not condensing, will in concentrated form together with the remaining amount of steam, flow over into the second preheat exchanger 72, in which it is cooled and condensed by heat exchanging with the incoming liquid W, to which is hereby added a further temperature rise.
- valve 77 opens, and the gas/liquid mixture flows to the vessel 78, in which the gas phase is separated from the liquid phase in the gas/liquid mixture in the second preheat exchanger 72.
- the gas is drained off and in vessel 78 a reservoir of liquid is built up until a certain level determined by level sensor 79, after which valve 80 opens and the liquid flows to the process vessel 41, in which it is mixed with the liquid under evaporation and cleaning.
- Fig. 4 shows that part of the plant in Fig. 3 that in concentrated form visualizes the invention, which thus combines an abso ⁇ tion column with a heat exchanger in which the condensate runs in counterstream with the steam which is to be condensated with an evaporation system.
- Fig. 5 shows an example of an abso ⁇ tion column according to the invention, where a part of the condensate flows in countercurrent with the steam flowing from below.
- the surface of the column elements is giving place for a number of acid/base reactions.
- Fig. 6 shows a heat exchanger according to the invention. On the figure is shown a downdraught evaporation heat exchanger, in which the condensing steam flows coun- tercurrent to its own condensate.
- first section of heat exchanger 11 second secton of heat exchanger 12: third heat exchanger 13 : first motor valve 14: second motor valve
- valve which by opening permits the liquid to flow further to the process vessel 41
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2000593087A JP2002537086A (en) | 1999-01-15 | 2000-01-14 | Method and apparatus for purifying wastewater |
AU30334/00A AU3033400A (en) | 1999-01-15 | 2000-01-14 | Process and apparatus for cleaning of waste water |
KR1020017008673A KR20010101436A (en) | 1999-01-15 | 2000-01-14 | Process and apparatus for cleaning of waste water |
CA002360349A CA2360349A1 (en) | 1999-01-15 | 2000-01-14 | Process and apparatus for cleaning of waste water |
EP00900498A EP1204854A2 (en) | 1999-01-15 | 2000-01-14 | Process and apparatus for cleaning of waste water |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DKPA199900038 | 1999-01-15 | ||
DK199900038A DK173837B1 (en) | 1999-01-15 | 1999-01-15 | Process and apparatus for purifying wastewater |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2000041462A2 true WO2000041462A2 (en) | 2000-07-20 |
WO2000041462A3 WO2000041462A3 (en) | 2001-11-29 |
Family
ID=8089039
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/DK2000/000013 WO2000041462A2 (en) | 1999-01-15 | 2000-01-14 | Process and apparatus for cleaning of waste water |
Country Status (7)
Country | Link |
---|---|
EP (1) | EP1204854A2 (en) |
JP (1) | JP2002537086A (en) |
KR (1) | KR20010101436A (en) |
AU (1) | AU3033400A (en) |
CA (1) | CA2360349A1 (en) |
DK (1) | DK173837B1 (en) |
WO (1) | WO2000041462A2 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2003057630A1 (en) * | 2001-12-20 | 2003-07-17 | Gnd Water As | Device and method for destillation |
EP2421622A1 (en) * | 2009-04-20 | 2012-02-29 | Drystill Holdings Inc. | Combined vaporizing/stripping absorption module |
EP1945573B1 (en) * | 2005-10-26 | 2015-08-05 | Daniel Blanchette | Water purification method, process and apparatus |
US9360252B2 (en) | 2011-03-08 | 2016-06-07 | Drystill Holdings Inc. | Process and apparatus for removing heat and water from flue gas |
US9931582B2 (en) | 2011-03-08 | 2018-04-03 | Drystill Holdings Inc. | Process and apparatus for removing heat and water from flue gas |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DK86894A (en) | 1994-07-22 | 1996-01-23 | Asger Gramkow | Method and apparatus for purifying gas |
DK171611B1 (en) | 1995-09-22 | 1997-02-24 | Envotech A S | Method for controlling a separation process and apparatus for use in the method |
DK128896A (en) | 1996-11-15 | 1998-05-16 | Funki Manura A S | Process and apparatus for separating volatile components from a liquid |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
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US4246417A (en) * | 1978-05-15 | 1981-01-20 | The Lummus Company | Treatment of waste water from nitrile production |
US4304638A (en) * | 1979-08-13 | 1981-12-08 | Vaponics Inc. | Distillation apparatus |
-
1999
- 1999-01-15 DK DK199900038A patent/DK173837B1/en not_active IP Right Cessation
-
2000
- 2000-01-14 KR KR1020017008673A patent/KR20010101436A/en not_active Application Discontinuation
- 2000-01-14 WO PCT/DK2000/000013 patent/WO2000041462A2/en not_active Application Discontinuation
- 2000-01-14 CA CA002360349A patent/CA2360349A1/en not_active Abandoned
- 2000-01-14 AU AU30334/00A patent/AU3033400A/en not_active Abandoned
- 2000-01-14 JP JP2000593087A patent/JP2002537086A/en active Pending
- 2000-01-14 EP EP00900498A patent/EP1204854A2/en not_active Ceased
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DK86894A (en) | 1994-07-22 | 1996-01-23 | Asger Gramkow | Method and apparatus for purifying gas |
DK171611B1 (en) | 1995-09-22 | 1997-02-24 | Envotech A S | Method for controlling a separation process and apparatus for use in the method |
DK128896A (en) | 1996-11-15 | 1998-05-16 | Funki Manura A S | Process and apparatus for separating volatile components from a liquid |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2003057630A1 (en) * | 2001-12-20 | 2003-07-17 | Gnd Water As | Device and method for destillation |
EP1945573B1 (en) * | 2005-10-26 | 2015-08-05 | Daniel Blanchette | Water purification method, process and apparatus |
EP2421622A1 (en) * | 2009-04-20 | 2012-02-29 | Drystill Holdings Inc. | Combined vaporizing/stripping absorption module |
EP2421622A4 (en) * | 2009-04-20 | 2014-06-25 | Drystill Holdings Inc | Combined vaporizing/stripping absorption module |
AU2010239064B2 (en) * | 2009-04-20 | 2016-03-17 | Drystill Holdings Inc. | Combined vaporizing/stripping absorption module |
US9345987B2 (en) | 2009-04-20 | 2016-05-24 | Drystill Holdings Inc. | Stripping absorption module |
KR101772236B1 (en) | 2009-04-20 | 2017-08-28 | 드라이스틸 홀딩스 인크. | Combined vaporizing/stripping absorption module |
US9868076B2 (en) | 2009-04-20 | 2018-01-16 | Drystill Holdings Inc. | Stripping absorption module |
US9360252B2 (en) | 2011-03-08 | 2016-06-07 | Drystill Holdings Inc. | Process and apparatus for removing heat and water from flue gas |
US9931582B2 (en) | 2011-03-08 | 2018-04-03 | Drystill Holdings Inc. | Process and apparatus for removing heat and water from flue gas |
Also Published As
Publication number | Publication date |
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CA2360349A1 (en) | 2000-07-20 |
AU3033400A (en) | 2000-08-01 |
WO2000041462A3 (en) | 2001-11-29 |
DK173837B1 (en) | 2001-12-10 |
JP2002537086A (en) | 2002-11-05 |
EP1204854A2 (en) | 2002-05-15 |
KR20010101436A (en) | 2001-11-14 |
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