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WO2001083127A1 - Installation et procedures de decontamination - Google Patents

Installation et procedures de decontamination Download PDF

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Publication number
WO2001083127A1
WO2001083127A1 PCT/NZ2001/000068 NZ0100068W WO0183127A1 WO 2001083127 A1 WO2001083127 A1 WO 2001083127A1 NZ 0100068 W NZ0100068 W NZ 0100068W WO 0183127 A1 WO0183127 A1 WO 0183127A1
Authority
WO
WIPO (PCT)
Prior art keywords
stream
dehalogenation
procedure
site
fine
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.)
Ceased
Application number
PCT/NZ2001/000068
Other languages
English (en)
Inventor
Bryan Geoffrey Black
Bianca Kuipers
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ENVIRONMENTAL DECONTAMINATION Ltd
Original Assignee
ENVIRONMENTAL DECONTAMINATION Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from NZ50434100A external-priority patent/NZ504341A/xx
Priority claimed from NZ51052201A external-priority patent/NZ510522A/xx
Application filed by ENVIRONMENTAL DECONTAMINATION Ltd filed Critical ENVIRONMENTAL DECONTAMINATION Ltd
Priority to AU60816/01A priority Critical patent/AU6081601A/en
Publication of WO2001083127A1 publication Critical patent/WO2001083127A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D3/00—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances
    • A62D3/30—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D3/00—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances
    • A62D3/30—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents
    • A62D3/37—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents by reduction, e.g. hydrogenation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C1/00—Reclamation of contaminated soil
    • B09C1/08—Reclamation of contaminated soil chemically
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D2101/00—Harmful chemical substances made harmless, or less harmful, by effecting chemical change
    • A62D2101/20—Organic substances
    • A62D2101/22—Organic substances containing halogen

Definitions

  • the present invention relates to a method of decontaminating a site.
  • the present invention is directed to a method of decontaminating a site where a site matrix
  • topsoil, clay, etc. has been contaminated with a halo-organic contaminant such as one or more of the DDT isomers, dieldrin, PCBs, etc.
  • the present invention relates to a methodology applicable in a procedure that involves a method of dehalogenation as disclosed in our New Zealand Patent Specification No. 504341 or in the Patent Specification filed simultaneously herewith in the PCT claiming the same priority dates (the details of which are included by reference).
  • the present invention recognises an advantage can be derived by realising just where the contamination largely is in a site and to stream the materials based upon a selection and/or screening procedure such that only part of the material necessarily must be subjected to dehalogenation.
  • a preferred dehalogenation procedure is that which we have developed and which is disclosed in the aforesaid Patent Specification and the Patent Specifications being filed simultaneously herewith.
  • Alternative methodologies for a dehalogenation procedure include that of BIRKE (PCT/DE98/02787) or that of Technological Resources Pty Ltd (AU 9456892) the full content of which are here included by way of reference.
  • the invention consists in a method of dehalogenating a halo-organic contaminated site which comprises or includes excavating the contaminated site to derive the contaminated media, subjecting the excavated contaminated media to particle size separation to provide at least two streams, namely at least one stream of finer particle sizes ("fine stream(s)") and at least one stream of larger particle sizes ("large stream(s)”), subjecting the fine stream(s) to a dehalogenation procedure, (optionally) subjecting the large stream(s) to a particle reduction procedure, subjecting the fine stream(s) post the dehalogenation procedure and the (optionally particle size reduced) large stream(s) to a blending procedure, and at least one of: (i) site reinstatement with (a) that blend and/or (b) other fill, (i ⁇ ) disposal of that blend.
  • blend is used for site reinstatement or disposing of the blend.
  • a single fine stream eg; ⁇ 10 mm
  • two large streams eg; 10 mm - 20 mm and greater than 20 mm.
  • the blend is disposed of, other site reinstatement fill may be used.
  • the excavation can isolate clay from topsoil etc. and where clay layers are excavated such clay layers are dried and thereafter are treated as part of the fine stream.
  • said excavation identifies fine materials for the fine stream by one or both of a) screening and/or b) identification as clay and each is preferably subjected to drying prior to onfeed into the dehalogenation procedure.
  • clay layers are subjected to solar drying, preferably also along with any fines from a particle size reduction procedure for at least one larger particle stream of said large stream(s).
  • Preferably only the fine layer(s) are subject to the dehalogenation process.
  • the dehalogenation process is a reactive milling process; ideally in a ball mill.
  • the milling involves either iron sands or steel makers slag, preferably in the presence of urea, and optionally in the presence of acetic acid.
  • the present invention consists in a blended material produced in a process as aforesaid.
  • the present invention consists in a material of blended particle streams, the fines stream or streams (unlike the non fines stream or streams) having been subjected to a dehalogenation procedure.
  • said material is of a kind as results from a methodology as previously stated.
  • the present invention consists in a method substantially as herein described with reference to any one or more of the accompanying drawings.
  • This invention may also be said broadly to consist in the parts, elements and features referred to or indicated in the specification of the application, individually or collectively, and any or all combinations of any two or more of said parts, elements or features, and where specific integers are mentioned herein which have known equivalents in the art to which this invention relates, such known equivalents are deemed to be incorporated herein as if individually set forth.
  • Figure 1 is a flow diagram showing three streams, one of which is the fine stream (0 to 10 mm particle size) and two of them large particle size streams (say 11 to 20 mm particle stream and a ⁇ 20 mm particle stream), the flow diagram showing how the fine stream is subjected to dehalogenation whilst the larger streams are preferably subject to particle size reduction (but not to the fineness of the dehalogenated material post reactor) prior to blending to provide a more stable site reinstatement blend of material than would be the case were the fine stream alone used for site reinstatement post dehalogenation
  • Figure 2 is a more detailed description of the procedure of Figure 1 showing on site separation of clay materials from top soil materials and how it is that the clay is dealt with in relation to the remainder of the process and additionally showing more detail in a treatment site for positioning at or adjacent a site to be decontaminated,
  • Figure 3 is a plan diagram of a readily created site to treat soils et al adjacent thereto, details of transportable units being given,
  • Figure 4 is a perspective view of a site layout as shown in Figure 3,
  • Figure 5 is a similar view to that of Figure 4 but showing with the added “enclosures” the areas to preferably be subjected to dust control,
  • Figure 6 shows again by "enclosures” those regions preferably to be subject to a measure of noise control (eg; the control office to protect it from ambient noise and the ball mill based reactor to reduce noise dissemination), and
  • a measure of noise control eg; the control office to protect it from ambient noise and the ball mill based reactor to reduce noise dissemination
  • Figure 7 is a diagrammatic view of a preferred reactor in accordance with the present invention.
  • the preferred dehalogenation procedure is preferably one that in a mobile ball mill (preferably with balls of less than 30 mm diameter (more preferably about 20 mm diameter)) is energised by its own dedicated prime mover and is adapted to be fed by portable plant the appropriate reactant stream to be milled with the fine stream of preferably 0 to 10 mm topsoil particles plus any dried clay materials that may warrant feeding through the dehalogenation procedure (see Figure 2).
  • the dehalogenation involves milling with either iron sands or steel makers slag preferably in the presence of urea and optionally also the presence of an organic acid (such as acetic acid, eg; white vinegar).
  • the solid stream is preferably subjected to crushing but there are options here of not crushing the smaller of one or more larger particle streams and/or subjecting one or other of the larger particle streams to washing etc. in case there is a desire to apply any dehalogenation procedure to the slurry to be forthcoming from any such washing. Preferably however washing is unnecessary.
  • the blending is in any appropriate mixer such as those frequently used for mixing concrete.
  • the apparatus that might be utilised is preferably shown in Figures 3 through 6. Figure
  • the apparatus shown in Figure 7 is a two chamber KHD Humboldt Wedag AG Palla 65U unit driven by a direct drive (1:1) clutched drive. Whilst an overcentre clutch with a twin disc is preferably used instead the drive could be through a torque convertor. Preferably the empowerment of the drive is with a diesel engine rated from a minimum
  • the rotary trommel accepts product ⁇ 20mm, and discharges product >10mm to a washing plant, with the ⁇ 10mm product being transferred by auger/conveyor (to be determined) to the rotary drier.
  • the supply of product to the rotary trommel (to be done by others - the product rate is to be advised in both tonnage, cubic metres and specific gravity). It is assumed that the >20mm/m may be washed and the sediment will be subject of a solar treatment process to be operated on site, the materials handling and subsequent feeding to the blending plant to be determined.
  • Oversize product is moved to the post process blender to restore our GEOTECHTM standards to sub micro processed product.
  • the rotary drier accepts from an auger feed, through the centre of the rotary drier, ⁇ 10mm product with moisture contents varying from 30% to 5%.
  • the requirement will be to produce product dried to ⁇ 2%, with the drying chamber not to exceed 70°C.
  • Air discharge is connected to the bag house in the reactor cell, with twin drop boxes in the ducting.
  • the drier be operated on a timer depending on requirements so that daily product is dried for the next day's production.
  • Three load hoppers are sited at ground level, low enough for front-end loader to feed product.
  • Product is screw fed from the bottom of each hopper and fed to an elevator to deliver it into various bulk hopper containers.
  • the bulk hopper is a "mass flow design" and is complete with a vibratory feeder mounted to the base.
  • High and low sensors are fitted to the bulk hopper with a visual warning for the operator to fill the hopper.
  • an actuated valve is used to control the product dump into a loss and weight feeder. This fills the feeder to present limits.
  • the loss and weight feeder is complete with an accurate weight system, which continuously monitors the flow rate from the feeder and automatically adjusts as required.
  • the product enters a continuous mixer, and once thoroughly mixed with the appropriate reagents is transferred to the reactor at a controlled rate, via vertical auger.
  • the product can be fed at variable production speeds from 2 tonnes/hour to 12 tonnes/hour.
  • the relationship of main product to reagents can be varied from 2% to 12%.
  • Reagent silos are designed to accommodate approximately one week's production so they can be bulk loaded.
  • the main product silo is designed to handle a minimum of 1.5 days production.
  • the stop/start of the entire plant and blending ratios is controlled via a PLC in the control room.
  • the mixing auger is a loose item as is the vertical screw conveyor.
  • the Reactor preferably as shown in Figure 7 accepts dried product of ⁇ 2% moisture content, which has been blended to the required percentages with the appropriate reagents, depending on contamination levels.
  • Product continues along the outer chamber, and discharges, to the product out-feed screw conveyor to the wet dosing plant.
  • the reactor is driven once by a rotating diesel engine producing about 475bhp.
  • the entire plant is encased in an acoustic airtight container, with an in-built bag house and air emission extractor fan system.
  • the rotary trommel 1 (is a 20ft ISO) transportable unit
  • the rotary drier 2 a 40ft ISO transportable unit
  • the reactor 4 a 40ft ISO transportable unit
  • the outfeed discharger a 40ft ISO unit
  • the bins by their very nature readily transportable, eg; 30m 2 bins
  • the control office itself preferably being a readily transportable building structure.
  • FIG. 7 there is shown a heavy chassis 7 from which static pedestals 8 project. It is on these pedestals 8 that flexible pads 9 are positioned which in turn support the ball mill 29 by virtue of it lateral extensions 10 thereof. This confinement between banks of pedestals 8 of the preferred ball mill (for example, a
  • KHD Humboldt Wedag AG Palla 65U twin chamber ball mill is such as to minimise the vibrating mass to be stabilised by the "static" counterweight mass of the engine, etc. and the chassis, pedestals, etc.
  • the direct drive at 16 to the eccentric(s) [not shown] is via a clutch 17 (preferably an overcentre twin disc clutch) from the engine 18.
  • the engine preferably is a GM Detroit Diesel 8V71 capable of producing approximately 600 bhp and a torque output of 3500NM.
  • the mill operates at 1200RPM of shaft 16 and thus the engine after having overcome the peak torque requirement on shaft 16 of about 3396NM at 150RPM.
  • a braking mechanism 19 is also provided such that the rotation of the drive 16 can be halted to damp excessive fibrations during wind down.
  • the unit preferably to a 40ft ISO transportable unit size preferably includes an extractor fan 19 and filters 20.
  • a simple baffle type wet scrubber installed in the rear of the container achieves the emissions of odours from this process.
  • This extracted air passes through a saw-tooth baffle, which creates a whitewash scrubber action, similar to a Venturi scrubber. There is no water pump required to achieve this progress.
  • the extraction fan with its high volume capabilities will extract the water through the baffles alone.
  • the extracted air which is entering the scrubber, has originated from the opposite end of the container.
  • a baffle forms an air gap between the exit point of the conveyor and the baffle. This provides an extraction rate of 6.6m/sec through the slot. This will maintain the dry airborne dust within the prolonging saturated period.
  • a slow cross draught down the length of the container will exist at approximately 0.3m/sec. This will carry a small percentage of sub-micron particles, along with water vapour within the container.
  • the fan would exhaust vertically at a rate of 18m/sec to assist in the dilution of odour emissions.
  • the complete system with the exception of the conveyor between the reactor and the scrubber container will be housed inside a 40ft ISO. All manufactured panels, fans, and scrubbers are of stainless steel.
  • Control Office The entire plant can be operated from a remote control office connected by umbilical cords. This means that the starting of the rotary trommel for the particle separation, the rotary drier, all blending plant and ratios, and the stop/start of the reactor and the out feed product conveyors are all separate stop/start switches.
  • the control office will be air conditioned, and will be video linked to all of the associated modules.
  • the preferred dehalogenation procedures are preferably milling procedures preferably using a milling procedure which has a higher energy than a rod mill procedure.
  • ball milling includes within its ambit alternatives to a strict ball form which nonetheless has an energy approaching that of ball milling.
  • iron sand includes any appropriate iron sand for the procedure. All such iron sands are preferably titanoferromagnetite sands. One such sand is that of, for example, BHP New Zealand Steel Limited having a content substantially as set out in Table 1 (being an analytical report of two samples).
  • Reference hereto to "steel makers slag” includes any suitable slag with iron or titanium values but preferably is a slag with both iron and titanium values such as that of BHP New Zealand Steel Limited.
  • the slag such as that set out in Table 2 is preferably post-crushing, and magnestic extraction of any zero oxidation state values initially present prior to oxidation thereof.
  • Table 2 is an example of BHP New Zealand Steel Gap 10 slag. TABLE 1: Iron Sands
  • the Fe values are present as oxides or other than zero oxidation state values.
  • the mill was then discharged, and urea (1.05 kg) and iron sand (700 g) were mixed into the soil.
  • the mill was reloaded, and the mixture milled for a further 30 minutes.
  • the mill temperature was above 70°C for the entire procedure.
  • GC-ECD analysis showed a 99% reduction in DDT levels, and a 99.7% reduction in dieldrin levels. No other halo-organic substances were detected.
  • GC-ECD analysis showed a 98.4% reduction in DDT levels, and a 99.7% reduction in dieldrin levels. No other halo-organic substances were detected.
  • Example 4 Soil (7 kg) contaminated with DDT (390 mg/kg dry weight) and dieldrin (71.4 mg/kg dry weight) was mixed with iron sand (1.40 kg), calcium sulphate (700g) and urea (700g). The soil was undried and had a moisture content of 9.3%>. This mixture was placed in a vibratory ball mill and milled for 30 minutes. The mill was then discharged, and urea (350 g) and iron sand (350 g) were mixed into the soil. The mill was reloaded, and the mixture was ground for 15 minutes. The mill was then discharged again, and an additional batch of urea (350 g) and iron sand (350 g) was mixed into the soil. This mixture was milled for 15 minutes. The mill temperature was above 70 °C for the entire process.
  • GC-ECD analysis showed a 96.9% reduction in DDT levels, and a 98% reduction in dieldrin levels. No other halo-organic substances were detected.
  • a final batch of urea (350 g) and iron sand (700 g) was mixed into the soil, and the soil was once again fed through an open vibratory bore mill. The time taken for total mill discharge was 14 minutes. This mixture was milled for 15 minutes. The mill temperature was above 70 °C for the entire process.
  • GC-ECD analysis showed a 95.1% reduction in DDT levels, and a 90.9% reduction in dieldrin levels. No other halo-organic substances were detected.
  • Soil (6.62 kg, oven-dried and pre-milled) contaminated with DDT (720 mg/kg dry weight) and dieldrin (64 mg/kg dry weight) was mixed with iron sand (1.24 kg) and urea (1.24 kg). This mixture was placed in a vibratory ball mill and milled for 30 minutes. The top of the mill was then opened, and urea (662 g) was poured in on top of the soil. The mixture was then milled for a further 30 minutes.
  • GC-ECD analysis showed a >99% reduction in DDT levels, and a >97% reduction in dieldrin levels. No other halo-organic substances were detected.
  • Soil (3.2 kg, oven-dried) contaminated with DDT (868 mg/kg) and dieldrin (64 mg/kg) was mixed with magnesium filings (160 g) and milled for 10 minutes. Butylamine (160 g) was then added and the mixture was milled for a further 10 minutes.
  • sample (IT) was replaced with ferrous balls of substantially similar mass, and another 5% of urea was added to sample (IT), and it was milled for a further 20 minutes.
  • Sample (III) was taken at the beginning of the discharge, sample (IV) was taken at the end of the discharge.
  • sample (IV) a further 5% of urea was added to sample (IV), and it was milled for a further 30 minutes (sample (V)).
  • sample (VI) a further 5% portion of urea was added to sample (V), and it was milled for a further 60 minutes (sample (VI)).
  • Example (A) Sydney clay (3 kg) (as used in Example 10) had iron sand (10%) and acetic acid (3%) added to it. The mixture was run through ball mill, and samples were taken after 40 min (Sample (A)).
  • Mapua soil with a mean contamination content in a less than 5 mm screened fraction of 71.9 mg/kg of dry weight Dieldrin and of 412 mg/kg of dry weight total of DDT isomers was then subjected to a milling procedure.
  • Contaminated soil as excavated was spread out on a tarpaulin and mixed well. Soil was then sieved through a 5mm sieve. The ⁇ 5mm fraction was collected and dried overnight in an oven kept at 50°C prior to use in the milling trials. The > 5mm fraction was used in soil washing trials. Approximately 43% of stockpile was ⁇ 5mm, and approximately 57% was > 5mm.
  • MCD Mechanochemical Dehalogenation Process
  • Soil (4kg of the oven-dried ⁇ 5mm fraction) was mixed with iron sand (200g, 5%) and acetic acid (2%). This mixture was introduced into the ball mill and milled for 30 minutes. The mill was the discharged, and a soil sample (150g) was taken. The milled soil was then mixed well with urea (400g, 10%) and iron sand (200g, 5%). This mixture was milled for a further 30 minutes. The mill was then discharged, and the soil was re-introduced into the mill (no extra reagent addition), and milled for another 30 minutes. A sample (150g) was taken for analysis. The above trial was carried out in triplicate (Runs A, B and C). Results are shown in Table 8. TABLE 8 - Results from Trial Carried Out in Triplicate (Runs A, B & C):
  • dieldrin In respect of dieldrin, the same can be said, where initial concentrations have varied from 80 mg/kg to 70 mg/kg. First stage results generally are down to the region of 10 mg/kg.
  • the general chemical composition of the BHP New Zealand Gap 10 slag is as follows: SiO 2 - 11.32% TiO 2 - 31.34% MgO - 12.76% CaO - 15.98% Total Fe values - 8.45% Al 2 O 3 - 16.88% V 2 O 3 - 0.28% MnO - 0.88% S - 0.18%
  • the material was mixed with 10% of the SR3 slag, 5% of unfiltered white vinegar (10% concentrate) and 5% urea.
  • the mill was operated for 20 minutes.
  • the Run 1 sample was extracted.
  • the material was mixed with 10%) unscreened slag sand, 5% unfiltered white vinegar (10% concentrate) and 5% urea.
  • the material was mixed with 10% of Gap 10 slag (ie, screened to particle size less than 10 mm), unfiltered white vinegar (10% concentrate) and 5% urea.
  • the mixed product was sampled to provide the spiked sample.
  • Material will be excavated from agreed contamination zones, to designated depths by a tracked excavator, having a wide bucket, with a sharp cutting edge.
  • Post excavation transport product is fed on to a primary screen where the oversize rock (> 100mm) will be stockpiled. Subject to further analysis (this has not been done because the representative sample was screened to ⁇ 50mm), if contamination levels require remediation, this sized product can be either washed, or crushed and run through the dehalogenation plant. If this product meets a satisfactory standard, subject to client specifications, it can be crushed and used as fill or placed as base course.
  • the process diagram incorporates a washing system, and if needed a simple trommel is used. Product screened to ⁇ 50mm will is placed in a dry trommel, and screened to ⁇ 5mm, prior to loading into the MCD Plant.
  • Product > 5mm is washed in a wet trommel, where the extracted sediment is rotary dried and joins the ⁇ 5mm particle sizing.
  • the > 5mm washed product is crushed to chent preference, sizing and also replaced on site as base fill and/or be part of the end product homogenized mix.
  • Identifying specific clay seams, during excavation is important. Physical clay seam separation during excavation for separate drying reduces processing costs. Pre-drying would be of a passive type, in a dedicated fully enclosed shed, constructed on site, similar to a commercial vegetable growers hothouse. An air extraction dust collection system will be installed.

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  • General Chemical & Material Sciences (AREA)
  • Business, Economics & Management (AREA)
  • Chemical & Material Sciences (AREA)
  • Emergency Management (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Toxicology (AREA)
  • Soil Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Environmental & Geological Engineering (AREA)
  • Engineering & Computer Science (AREA)
  • Fire-Extinguishing Compositions (AREA)

Abstract

L'invention concerne une méthodologie applicable dans un procédé de décontamination d'un site présentant des contaminants halo-organiques. Ledit procédé consiste à creuser le site contaminé pour dériver les milieux contaminés, à faire subir aux milieux contaminés extraits du sol une séparation granulométrique, de façon à obtenir au moins deux flux, à savoir au moins un flux de petites particules ('petit(s) flux') et au moins un flux de grosses particules ('gros flux'), et, en particulier, à faire subir au(x) flux de petites particules une procédure de déshalogénation puis à le mélanger au(x) gros flux.
PCT/NZ2001/000068 2000-05-03 2001-05-02 Installation et procedures de decontamination Ceased WO2001083127A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU60816/01A AU6081601A (en) 2000-05-03 2001-05-02 Decontamination plant and procedures

Applications Claiming Priority (10)

Application Number Priority Date Filing Date Title
NZ504341 2000-05-03
NZ50434100A NZ504341A (en) 2000-05-03 2000-05-03 Decontaminating a media such as soil of organo halogen compounds such as DDT
NZ510521 2001-03-12
NZ51052201A NZ510522A (en) 2001-03-12 2001-03-12 Decontaminating a media such as soil of organo halogen compounds such as DDT
NZ510522 2001-03-12
NZ51052101 2001-03-12
NZ510752 2001-03-23
NZ51075201 2001-03-23
NZ51082401 2001-03-28
NZ510824 2001-03-28

Publications (1)

Publication Number Publication Date
WO2001083127A1 true WO2001083127A1 (fr) 2001-11-08

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Family Applications (2)

Application Number Title Priority Date Filing Date
PCT/NZ2001/000069 Ceased WO2001083038A1 (fr) 2000-05-03 2001-05-02 Detoxification de composes halogenes dans un milieu contamine
PCT/NZ2001/000068 Ceased WO2001083127A1 (fr) 2000-05-03 2001-05-02 Installation et procedures de decontamination

Family Applications Before (1)

Application Number Title Priority Date Filing Date
PCT/NZ2001/000069 Ceased WO2001083038A1 (fr) 2000-05-03 2001-05-02 Detoxification de composes halogenes dans un milieu contamine

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AU (2) AU6081601A (fr)
WO (2) WO2001083038A1 (fr)

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WO2007105972A1 (fr) 2006-03-15 2007-09-20 Mcd Technology Limited APPAREIL de fraisage
WO2014032211A1 (fr) * 2012-09-03 2014-03-06 清华大学 Procédé de traitement chimique de déchets solides de composés perfluorés et polyfluorés en utilisant une force mécanique
CN111168171A (zh) * 2020-03-16 2020-05-19 沈阳飞机工业（集团）有限公司 超塑成形/扩散连接零件化铣方法

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ITMI20121827A1 (it) * 2012-10-26 2014-04-27 Biodermol S R L Processo per la decontaminazione di terreni inquinati da insetticidi
CN106807735A (zh) * 2017-01-24 2017-06-09 中石化炼化工程（集团）股份有限公司 一种污染土壤修复系统和污染土壤修复的方法
CA3039965A1 (fr) 2019-04-10 2020-10-10 Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of National Defence Methode pour assainir le sol contamine au polyfluorocarbure
CN112730651B (zh) * 2020-12-15 2022-08-05 湖北微谱技术有限公司 一种二噁英样品快速前处理方法
CN114054472B (zh) * 2021-10-22 2023-09-19 中石化宁波工程有限公司 一种降解含卤有机污染物的方法
CN115261631A (zh) * 2022-08-10 2022-11-01 贵州大学 一种电解金属锰阳极渣回收处理方法

Citations (8)

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