WO2002036502A1 - Waste treatment process - Google Patents
Waste treatment process Download PDFInfo
- Publication number
- WO2002036502A1 WO2002036502A1 PCT/AU2001/001397 AU0101397W WO0236502A1 WO 2002036502 A1 WO2002036502 A1 WO 2002036502A1 AU 0101397 W AU0101397 W AU 0101397W WO 0236502 A1 WO0236502 A1 WO 0236502A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- waste
- component
- bioreactor
- solids
- nitrogen
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/286—Anaerobic digestion processes including two or more steps
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5254—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using magnesium compounds and phosphoric acid for removing ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1205—Particular type of activated sludge processes
- C02F3/1215—Combinations of activated sludge treatment with precipitation, flocculation, coagulation and separation of phosphates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- 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
- Y02W10/10—Biological treatment of water, waste water, or sewage
Definitions
- THIS INVENTION relates to a waste treatment process and plant, which is suitable for treatment of waste inclusive of biological waste exemplified by faeces, sewage and household waste and commercial and industrial waste.
- WO 95/25071 which refers to waste treatment plant and process, which includes the steps of:
- step (iii) separating the insoluble component from the waste material before or after step (ii).
- US Patent 5,993,503 refers to a process for removal of phosphorous from fresh manure, which includes the steps of: (i) storing the fresh manure comprising solids and liquid for a period of at least one month at a temperature between 0-15°C, or for a period of at least one week subjected to continual agitation at a temperature above 15° C, to cause phosphorous to dissolve into the liquid component out of the solids; (ii) preventing precipitation of phosphate out of the liquid during step (i) by any one of the following methods;
- An object of the invention is to provide a method of waste treatment involving removal of phosphorous and/or nitrogen, which at least reduces the disadvantages of the prior art discussed above. 5 I n accordance with the invention there is provided a process of waste treatment which includes the following steps:
- an aeration step is carried out in respect of the waste material either before or after step (e).
- the aeration 5 step is carried out after step (e) in respect of the concentrated solids component.
- the solids removed from the concentrated solids component in step (e) may be used as compost additive, soil conditioner or landfill as appropriate.
- step (a) the waste may have a solids content of 0.5-2.0% o w/v.
- the predominantly solids component may have a solids content of 3.0-8.5% w/v and more usually around 4-6% w/v.
- step (d) it is preferred to chemically remove nitrogen and/or phosphorous from the predominantly liquid component i.e. step (c) rather than the concentrated solids component, i.e. step (d).
- steps (c) and (d) will be carried out with usually step (d) occurring before step (c) although the reverse may also occur.
- the predominantly liquid component may be held in a holding tank or lagoon for a considerable time, 24 hours to several months for example, before nitrogen and phosphorous are removed.
- the waste material in some circumstances will have a pH of around 5.3-5.8 and thus may have to be subjected to a pH lowering step when passing through the anaerobic bioreactor system. More preferably, the pH lowering step will take place in a final bioreactor of the bioreactor system. However, it will be appreciated that the pH lowering step may be applied to other bioreactors. However, it will be appreciated that in some circumstances, because of the nature of the waste material, a pH lowering step may not be necessary.
- the pH lowering step will involve the addition of a strong mineral acid such as hydrochloric acid, sulphuric acid or nitric acid.
- a strong mineral acid such as hydrochloric acid, sulphuric acid or nitric acid.
- this does not preclude the use of other acids such as phosphoric acid, perchloric acid or strong organic acids, which will achieve the same effect.
- the bioreactor system may comprise a plurality of bioreactors as described in WO 95/25071 the contents of which are totally incorporated herein by reference.
- each bioreactor may be interconnected by an overflow conduit so that waste material or effluent is quickly and efficiently transferred from one bioreactor to an adjacent bioreactor without the need for pumping material so as to transfer material from one bioreactor to another.
- each bioreactor is provided with agitation means, which keeps the contents of each bioreactor in the form of a slurry or suspension, so that solid particles are maintained in a suspended state.
- each bioreactor may be also subject to heating means and in one form this may be provided by steam being passed into and out of each bioreactor.
- heating means may be adopted, such as electrical heating.
- the temperature in each bioreactor is maintained by suitably thermostatically controlled means between 25-40°C and more suitably 30-40°C.
- the pH of each of the bioreactors is maintained between 5.0-6.0 and more preferably 5.8, except in the case where a pH lowering step is applied to specific bioreactor(s).
- the retention time in each bioreactor may be 12-48 hours, but more suitably is 24 hours.
- the waste material which is subject to the process of the invention, may comprise human or animal faeces and preferably faeces from livestock feedlots, which may have a stockfeed component containing lignocellulose.
- the process of the invention is extremely efficient in treatment of waste which requires an initial anaerobic fermentation step to break down complex macromolecules such as carbohydrates and proteins to short chain organic acids of 8 carbon atoms or less. Also complex macromolecules such as lipids may be broken down to long chain organic acids of 9 carbon atoms or more and glycerol.
- This fermentation step usually takes place in the presence of acidogenic fermentative bacteria and lipolytic bacteria which can produce organic acids such as volatile fatty acids and long chain fatty acids, which may be readily metabolised to carbon dioxide and water.
- anaerobic bioreactors as described above which are designed so that oxygen or air is prevented from being introduced into each of the bioreactors.
- the amount of dissolved oxygen will be very low and be less than 0.7mg/l.
- Such bioreactors therefore may be sealed from atmosphere.
- the waste so treated may then be passed to an aerobic tank or aerated system.
- It may comprise one cell or a plurality of aerobic or aerated cells wherein an air line may supply air or oxygen to aerators or jets, which feed the air under pressure into the cell(s).
- aerators may function under diffusion but mechanical aerators may also be utilised.
- the aerator may be of plug- flow configuration as described in US Patent 5,380,438 or may be of a step- feed and complete-mix aeration configuration or alternatively an activated sludge system.
- the aeration system may comprise a tank having a submersible pump or agitator in which air is fed into the tank under pressure.
- the waste material after passage from the anaerobic bioreactor system may be subjected to a separation procedure to remove a solid component such as sludge.
- the separation procedure is applied to the waste material preferably prior to aeration. This may be achieved by passing the waste material over a screen, which is subject to the action of wash water above and below the screen, to prevent clogging or blockages occurring in pores or passages located in the screen.
- a filter system known as the BAYLEEN filter system, which is described in International Publication 98/23357, which is incorporated herein by reference.
- FIG. 1 refers to a flow sheet corresponding to the process of the invention.
- FIG. 2 refers to a flow sheet corresponding to the process of the invention.
- the aeration step as applied to the solids concentrate after filtration is optional.
- FIG. 2 shows another preferred embodiment of the invention as shown in the attached drawing in FIG. 2, wherein initially, faeces from an animal feedlot or commercial or industrial waste, are delivered to a loading bay 10, wherein waste may be conveyed to holding tanks 14A, 14B and 14C along conduits 11 , 12 and 13 respectively.
- Loading bay 10 may also comprise a macerator pump for transporting waste to holding tanks 14A, 14B and 14C.
- Each of the holding tanks 14A, 14B and 14C may be used for different kinds of waste material e.g. faeces from animal feedlots in tank 14A, dairy waste in tank 14B and sewage waste in tank 14C.
- each tank may be used to store the same kind of waste or mixture of wastes.
- waste from each of tanks 14A, 14B and 14C is pumped by pump P1 along separate conduits 15, 16 and 17, each having valves V1 , V2 and V3.
- Pump P1 after collecting the waste from conduits 15, 16 and 17 may transfer the collected waste to concentration zone 18A through conduit 18.
- each of conduits 15, 16 and 17 may be provided with their own pump for transfer of fluid to concentration zone 18A.
- the waste may be passed through a filter as described herein, parabolic steel screen, or have a flocculating agent such as Alum or Ferric Chloride added thereto or other reagent to concentrate the solids.
- a solid concentrate may then be passed to bioreactor and predominantly liquid component is passed through a drain (not shown) from zone 18A to holding tank or lagoon 18C through line or conduit 18B.
- Nitrogen and phosphorous may be removed in treatment tank 18D before being passed out through conduit 18E for reuse or ultimate disposal.
- the waste may be maintained at a pH of around 5.0-6.0 or more suitably 5.8.
- the average dry weight of solid material discharged into bioreactor 19 will be of the order of 3.0-8.5% dry weight w/v and more preferably 5.0% dry weight w/v.
- lipolytic bacteria which hydrolyse triacylglycerols or triglycerides to yield free long chain fatty acids and glycerol and are exemplified by bacteria of the genus Veillonella and Anerovibrio, which are found in faeces.
- the faeces may also contain proteolytic bacteria, which convert the majority of the protein to branched chain volatile fatty acids and ammonia nitrogen.
- proteolytic bacteria which convert the majority of the protein to branched chain volatile fatty acids and ammonia nitrogen.
- Such bacteria may include Bacteroides, Clostridia and Bifidobacterium and are commonly found in faeces.
- Saccharolytic bacteria also found in faeces convert carbohydrate to straight chain volatile fatty acids and may include Clostridia, Butyrivibrio, Streptococcus, Bacteroides and Megasphera elsdenii. Faeces also contain facultative anaerobes, which are active in oxygen rich atmosphere or atmospherewhich is depleted in oxygen and are exemplified by Enterobacteriacae. Such bacteria reduce oxygen present in the fermentation liquor.
- Faeces also contain hydrolytic fermentative and acid forming bacteria, which produce volatile fatty acids.
- Such volatile fatty acids may include acetic acid, proprionic acid, butyric acid, valeric acid, caproic acid, heptanoic acid and octanoic acid. Branched volatile fatty acids may also be produced such as isobutyric acid and isovaleric acid.
- elements comprising N, S, C, P and K as well as Mg, Ca, Na and Cl " .
- a rich source of N, P and K is agricultural fertiliser inclusive of meatmeal, blood and bone, urea and superphosphate.
- a preferred source of N is ammonium hydroxide and preferably 0.5-5.0 ml/litre of waste is added to bioreactor 19. Most preferably this is 2ml/litre.
- ammonium hydroxide has a strength of 25% ammonia. It is emphasised that the content of the waste stream entering bioreactor 19 is extremely variable and thus should be monitored to check whether the abovementioned elements should be added. If necessary in the case of sewage waste faeces may be added to bioreactor 19 and this may comprise physiologically active faeces, such as untreated human sewage.
- the waste is then transferred to bioreactors 21 , 23, 25 and 27 through lines 20, 22, 24 and 26.
- acid suitably in the form of industrial strength sulphuric acid may be added . This will lower the pH to 5 around 4.0-4.7 and more suitably 4.3 to promote the action of the free VFAs described above in killing bacterial pathogens in the waste. This pH is maintained for a period of at least 24 hours. Preferably 1-10ml of acid per litre of waste is added and more preferably this is 5ml/litre. Usually the acid is industrial grade i.e. 50% strength.
- the waste may then be passed through treatment zone 27A wherein nitrogen and/or phosphorous may be physically, chemically or biologically removed.
- nitrogen and/or phosphorous may be physically, chemically or biologically removed.
- magnesium hydroxide, calcium hydroxide or other alkaline earth metal hydroxide may be added to the liquid waste to cause 5 precipitation of calcium phosphate or magnesium phosphate.
- magnesium hydroxide may be added to the waste which will react with any phosphorous present as well as nitrogen present as ammonia to cause precipitation of struvite i.e. MgNH 4 PO 4 .6H 2 0.
- Nitrogen may be captured from the liquid waste by addition of a mineral acid such as sulphuric acid, which may react with any ammonia in the waste to form ammonium sulphate. Nitrogen in the form of ammonia may also be removed by nitrification followed by denitrification e.g. by means of micro-organisms. 5 The process as described above also applies to treatment zone
- the fermented waste including any indigestible solids may be transferred to aeration vessels 31 , 33 and 35.
- aerobic bacteria may be added 5 such as Acinetobacter sp. to remove N and P..
- appropriate nutrients such as nitrogen and other elements, as described above and in the same concentration, may be added to the aeration vessels so that the volatile fatty acids and long chain acids may be oxidised to carbon dioxide and water.
- the total time of aeration may be from 2-5 days and more preferably 5 days.
- i o Fermented waste may be transferred to a filter 29 along line 28 before the filtered waste enters aeration vessel 31 through line 30.
- Filter 29 is preferably a filter known as the BAYLEEN filter described above which is in the form of a stainless steel filter having apertures of around 30 -100 microns wherein a fine spray washes solids down the screen for ultimate
- screw press filters may be used or parabolic stainless steel screens.
- aerated waste after the aerated waste has passed through aeration vessels 31 , 33 and 35 through lines 32, 34 and 36 such aerated waste may be subjected to the action of filter 29A after passage of the waste through aerated vessel 35.
- This alternative may be preferable to use of filter 29 because if filtration takes place prior to aeration, a significant quantity of 25 VFAs and long chain fatty acids may adhere to the separated solids. This may provide a more active sludge for disposal and a weaker or more dilute residue solution to be oxidised by aeration vessels 31 , 33 and 35.
- Solids may be transported from filter 29 or 29A through line 29B to composting area 29C or transported from the treatment plant.
- the dry weight solids in the raw waste have been reduced by about 50% and the BOD of the raw waste has been reduced by about 90%.
- the aerated liquid may be held in holding tank 37 for a period of time (12-24 hours) prior to optional passage to tank 39 through line 38. Subsequently the aerated liquid may be transferred through lines 40 and 41 to wetlands or retention ponds as appropriate. Each of lines 40 and 41 are provided with valves V4 and V5.
- lines 40 and 41 are shown extending from tank 37 and this is appropriate when only a single holding tank is utilised. However, if tank 39 is used, lines 40 and 41 may be connected to this tank rather than tank 37.
- tanks 14A, 14B and 14C may be above ground plastics tanks of 45,000 litre capacity and maintained at a temperature of 20-40°C.
- the influent waste material may be piggery flume floor flushings having a solids size range of 2-5mm.
- the pH may be 5.8-6.4.
- the temperature of the influent waste material may be 20-30°C and have a design flow of around 73.5 l/hour.
- Each of the bioreactors 19, 21 , 23, 25 and 27 may be of the same structure as described in WO 95/25071 and hence are only shown in schematic form in FIG. 2.
- the temperature of each of the bioreactors may be maintained at a temperature of 37°C.
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2002213652A AU2002213652A1 (en) | 2000-10-30 | 2001-10-30 | Waste treatment process |
NZ526092A NZ526092A (en) | 2000-10-30 | 2001-10-30 | Waste treatment process |
EP20010981951 EP1347943A1 (en) | 2000-10-30 | 2001-10-30 | Waste treatment process |
US10/415,441 US20040065611A1 (en) | 2000-10-30 | 2001-10-30 | Waste treatment process |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AUPR1128A AUPR112800A0 (en) | 2000-10-30 | 2000-10-30 | Waste treatment process |
AUPR1128 | 2000-10-30 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2002036502A1 true WO2002036502A1 (en) | 2002-05-10 |
Family
ID=3825171
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/AU2001/001397 WO2002036502A1 (en) | 2000-10-30 | 2001-10-30 | Waste treatment process |
Country Status (5)
Country | Link |
---|---|
US (1) | US20040065611A1 (en) |
EP (1) | EP1347943A1 (en) |
AU (2) | AUPR112800A0 (en) |
NZ (1) | NZ526092A (en) |
WO (1) | WO2002036502A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014038965A1 (en) * | 2012-09-06 | 2014-03-13 | Harding Alan Robert | A method for treatment of waste water |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
TWI313187B (en) * | 2003-11-21 | 2009-08-11 | Ind Tech Res Inst | System for the treatment of organic containing waste water |
WO2005113456A2 (en) * | 2004-05-14 | 2005-12-01 | Northwestern University | Methods and systems for total nitrogen removal |
US20060194299A1 (en) * | 2005-02-04 | 2006-08-31 | Henrik Brinch-Pedersen | Method for recycling important nutritional elements from waste |
US7445707B2 (en) * | 2005-05-11 | 2008-11-04 | Envirolytic Technologies, Llc | Waste effluent treatment system |
US20080156726A1 (en) * | 2006-09-06 | 2008-07-03 | Fassbender Alexander G | Integrating recycle stream ammonia treatment with biological nutrient removal |
US20080053913A1 (en) * | 2006-09-06 | 2008-03-06 | Fassbender Alexander G | Nutrient recovery process |
US20080053909A1 (en) * | 2006-09-06 | 2008-03-06 | Fassbender Alexander G | Ammonia recovery process |
US7552827B2 (en) * | 2006-10-10 | 2009-06-30 | Envirolytic Technologies, Llc | Systems and methods of separating manure from a manure and bedding mixture |
US7713417B2 (en) * | 2007-03-16 | 2010-05-11 | Envirogen Technologies, Inc. | Method for wastewater treatment with resource recovery and reduced residual solids generation |
US20130134089A1 (en) * | 2011-11-30 | 2013-05-30 | General Electric Company | Method and system for treating wastewater |
WO2014130043A1 (en) | 2013-02-22 | 2014-08-28 | General Electric Company | Membrane assembly for supporting a biofilm |
AU2015231819B2 (en) | 2014-03-20 | 2019-05-16 | Bl Technologies, Inc. | Wastewater treatment with primary treatment and MBR or MABR-IFAS reactor |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4999111A (en) * | 1988-06-02 | 1991-03-12 | Orange Water And Sewer Authority | Process for treating wastewater |
US5022993A (en) * | 1988-06-02 | 1991-06-11 | Orange Water And Sewer Authority | Process for treating wastewater |
EP0484867A1 (en) * | 1990-11-09 | 1992-05-13 | ECOLMARE S.p.A. | Process for the utilization of organic wastes for producing biogas and agricultural products |
US5531898A (en) * | 1995-04-06 | 1996-07-02 | International Organic Solutions Corp. | Sewage and contamination remediation and materials for effecting same |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1989589A (en) * | 1934-05-31 | 1935-01-29 | Dorr Co Inc | Sewage digestion |
NL296691A (en) * | 1962-08-15 | |||
US3959125A (en) * | 1974-07-05 | 1976-05-25 | Sterling Drug Inc. | Treatment and disposal of sewage sludge |
US3930998A (en) * | 1974-09-18 | 1976-01-06 | Sterling Drug Inc. | Wastewater treatment |
US4375412A (en) * | 1979-01-15 | 1983-03-01 | Schimel Keith A | Methods for the treatment of organic material and particularly sewage sludge |
US4867883A (en) * | 1987-04-21 | 1989-09-19 | Hampton Roads Sanitation District Of The Commonwealth Of Virginia | High-rate biological waste water treatment process using activated sludge recycle |
US5922204A (en) * | 1992-08-04 | 1999-07-13 | Hunter; Robert M. | Method and apparatus for bioremediation of mixed hazardous wastes |
US5397473A (en) * | 1993-08-27 | 1995-03-14 | Cornell Research Foundation, Inc. | Biological treatment method for water |
NL9401495A (en) * | 1994-09-15 | 1996-04-01 | Ceres Milieu Holding Bv | Method and device for dephosphating pig manure. |
US5601719A (en) * | 1996-01-11 | 1997-02-11 | Black & Veatch | Biological nutrient removal process for treatment of wastewater |
EP0912450A4 (en) * | 1996-07-10 | 2000-11-15 | Aqua Aerobic Systems Inc | Multi-phase dual cycle influent process |
-
2000
- 2000-10-30 AU AUPR1128A patent/AUPR112800A0/en not_active Abandoned
-
2001
- 2001-10-30 WO PCT/AU2001/001397 patent/WO2002036502A1/en not_active Application Discontinuation
- 2001-10-30 EP EP20010981951 patent/EP1347943A1/en not_active Withdrawn
- 2001-10-30 AU AU2002213652A patent/AU2002213652A1/en not_active Abandoned
- 2001-10-30 US US10/415,441 patent/US20040065611A1/en not_active Abandoned
- 2001-10-30 NZ NZ526092A patent/NZ526092A/en unknown
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4999111A (en) * | 1988-06-02 | 1991-03-12 | Orange Water And Sewer Authority | Process for treating wastewater |
US5022993A (en) * | 1988-06-02 | 1991-06-11 | Orange Water And Sewer Authority | Process for treating wastewater |
EP0484867A1 (en) * | 1990-11-09 | 1992-05-13 | ECOLMARE S.p.A. | Process for the utilization of organic wastes for producing biogas and agricultural products |
US5531898A (en) * | 1995-04-06 | 1996-07-02 | International Organic Solutions Corp. | Sewage and contamination remediation and materials for effecting same |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014038965A1 (en) * | 2012-09-06 | 2014-03-13 | Harding Alan Robert | A method for treatment of waste water |
Also Published As
Publication number | Publication date |
---|---|
US20040065611A1 (en) | 2004-04-08 |
NZ526092A (en) | 2003-08-29 |
AU2002213652A1 (en) | 2002-05-15 |
AUPR112800A0 (en) | 2000-11-23 |
EP1347943A1 (en) | 2003-10-01 |
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