WO2001064587A2 - Procede et appareil pour realiser des traitements par oxydation tres efficaces - Google Patents

Procede et appareil pour realiser des traitements par oxydation tres efficaces Download PDF

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Publication number
WO2001064587A2
WO2001064587A2 PCT/CA2001/000261 CA0100261W WO0164587A2 WO 2001064587 A2 WO2001064587 A2 WO 2001064587A2 CA 0100261 W CA0100261 W CA 0100261W WO 0164587 A2 WO0164587 A2 WO 0164587A2
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WO
WIPO (PCT)
Prior art keywords
oxidation
stream
tubular reactor
gases
process stream
Prior art date
Application number
PCT/CA2001/000261
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English (en)
Other versions
WO2001064587A3 (fr
Inventor
Jerzy Stefan Janiak
Timothy John Hnatiw
Kenneth William Hnatiw
Ryan Richard Richardson
Michael Hillwood Diebel
Original Assignee
Micromining Technologies Int'l. Inc.
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Publication date
Application filed by Micromining Technologies Int'l. Inc. filed Critical Micromining Technologies Int'l. Inc.
Priority to AU2001239044A priority Critical patent/AU2001239044A1/en
Publication of WO2001064587A2 publication Critical patent/WO2001064587A2/fr
Publication of WO2001064587A3 publication Critical patent/WO2001064587A3/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C1/00—Reclamation of contaminated soil
    • B09C1/02—Extraction using liquids, e.g. washing, leaching, flotation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/02—Temperature
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • 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 present invention relates to a method and apparatus for achieving highly effective industrial oxidation of oxidizable compounds in a process stream.
  • Such applications involve the removal and/or neutralization and deodorizing toxic pollutants in the forms of inorganic and organic compounds from water, water slurries and solids.
  • the pollutants may originate from the waste streams from chemical, petroleum, mineral processing, food processing industrial facilities, municipal and farming wastes or hospital effluent and military, chemical and biological wastes.
  • the invention is capable of successfully oxidizing components in a chemical processing stream with full control of oxidation level in treating the stream.
  • Such treatments may involve ore treatment, for example, the recovery of gold or uranium.
  • the invention is capable of successfully removing such pollutants as hydrocarbons from drilling waste streams and spills, polychlorobiphenyls (PCB's) from transformers, pesticides, bacteria, viruses, and cyanides from gold mining processing.
  • PCB's polychlorobiphenyls
  • the cleaning and deodorizing process was also proven for wastes from animal farming. BACKGROUND OF THE INVENTION
  • oxidation processes are used which applied oxidation gases or compounds such as air, oxygen, ozone or hydrogen peroxide.
  • the reactors used to date are inefficient and uneconomic. So far, these processes are seldom used for cleaning water slurries and solids.
  • the next step was thermal decomposition, i.e. pollutant oxidation by a high temperature (-1 ,000°C) burning process.
  • the negative side of such process is the need for complicated and expensive furnaces.
  • the process is slow and requires additional fuel burning to produce heat. Consequently, it introduces additional CO 2 , SO 2 , and SO 3 pollutants into the environment in the amounts often much larger than those from the decomposition of the pollutants proper.
  • the burning process ensures a high-degree of decomposition and is still in frequent use but it has three drawbacks: • depletes oxygen in the environment as oxygen is used to burn fuel;
  • cyanide rejects from gold-ore processing mills are environmentally degradable, but this natural process requires temperatures much higher than 10°C, a steady supply of oxygen, sunlight (UV) and takes a long time. More importantly, the long process time often makes it possible for the cyanide pollutants to enter the water ecosystem. In the northern environment the period of time with enough temperature and sunshine, i.e. favorable to the natural decomposition, is short and a build-up of wastes occurs. This entails an enlargement of the polluted area and the necessity to construct additional large waste reservoirs. Consequently, birds and any aquatic life become endangered by their increased exposure to the contaminated water reservoirs.
  • a process for treating oxidizable compounds in a process stream comprising: i) introducing oxidation gases containing ozone to the process stream ii) pressurizing the process stream to a predetermined pressure after the oxidation gases are introduced to the process stream to increase solubility of oxidation gases in the process stream and penetration of oxidation gases into pores of process materials containing the oxidizable compounds; iii) directing the pressurized process stream through an extended tubular reactor to achieve a desired degree of oxidation of the oxidizable compounds in the process materials while maintaining the predetermined pressure in the tubular reactor and recirculating the process stream in the tubular reactor until the desired degree of oxidizable compound oxidation is achieved; iv) maintaining by periodic adjustments, pH of said process stream to increase production of oxidizing components in the pressurized process stream and neutralize acidic gases produced in the tubular reactor; and v) monitoring temperature of the pressurized process stream in the tub
  • an apparatus for oxidizing oxidizable compounds in a process stream to be treated in the apparatus comprising: i) a pump for pressurizing a process stream; ii) means for introducing an oxidation gas stream into an inlet side of the pump whereby such gas stream is dispersed throughout the process stream; and iii) a tubular reactor connected to an outlet of the pump, the tubular reactor being of sufficient length to achieve a desired degree of oxidation of such oxidizable compounds in the process stream.
  • Figure 1 is a schematic of the Oxidation Gas Generator
  • FIG. 2 is a schematic of the Reactor System. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS OF THE INVENTION
  • the present invention provides a new, effective and economical tubular reactor for the treatment of polluted water, water slurry, solids and any oxidizing process requiring very effective mass transfer.
  • This reactor system has the following characteristics which make it superior to the reactors conventionally used:
  • the invention provides: • methods to utilize air components to produce in-situ highly active oxidative gaseous compounds to be used for fast, complete and economical industrial oxidation processes such as decomposition of the pollutants, metallurgical processes (e.g. gold extraction) and the like and/or oxidization process component; • a very effective system for generation, supply and distribution of oxidation gases into the reaction zone of the reactor;
  • • acidic based components released in the cleaning process, such as, CO 2 , SO 3 , NO ⁇ , HCI may be simultaneously neutralized in processed slurry, by an alkaline component such as calcium hydroxide, sodium hydroxide and like compatible basic components.
  • the invention offers a technology with a much reduced secondary or byproduct pollutants resulting from the oxidized components released to the atmosphere as compared to the conventional thermal decomposition process now in wide use.
  • the main byproduct of the decomposition of the overdose of oxidation gases released to the atmosphere, is oxygen.
  • the invention may allow, in the initial steps of the process, for physical separation of the bulk of highly concentrated hydrocarbons by floatation in the conventional mixing section of the pretreatment reactor. This process also allows for recycling hydrocarbons and decreasing the oxidant gas consumption in the final stage of the oxidation process.
  • the invention offers the possibility of utilizing the existing reject slurry pipelines (for example, carrying gold mining cyanide rejects or uranium ore transportation in uranium production) as tubular reactors.
  • Oxidation gases from the Generator, Supply and Distribution System can be injected directly into the tubular reactor.
  • advanced oxidation process can be used in situ for extraction of uranium in underground mining. In gold refining, the system is particularly effective.
  • the oxidation gases of this invention are strong oxidants.
  • the introduction of the oxidation gases increases the rate of gold dissolution in the gold cyanidation slurry.
  • the efficient tubular reactor greatly enhances the effectiveness of leeching of gold from the ore.
  • the use of this system greatly reduces the amount of cyanide compound to that used in a conventional process
  • the invention provides a complete system to be used to clean, for example, contaminated water, water slurry, solids or any process requiring a highly oxidative treatment or sterilization of decontamination both in continuous load and/or batch load modes.
  • the simplicity of the invented system allows for designing and building it in compact stationary or compact mobile versions for industrial oxidation treatments.
  • the developed oxidation treatment uses the readily available components of air to produce highly active oxidation gases to decompose (neutralize) the pollutant compounds and to act as an oxidative reagent in industrial processes.
  • Such a treatment also makes it possible to utilize cleaning devices or pipelines that may already exist in the facilities on the polluted sites or industrial oxidative processes, such as metallurgical treatments.
  • the system consists of two subsystems.
  • the advanced oxidation gas generator consists of three principal units: 1. Electric power generator.
  • the contact reactor consists of four principal units:
  • the treatment system preferably has two mixing systems designed to provide: • A first vessel, pretreatment reactor, or the like which employs a conventional mixing and optionally a floatation unit allowing for three types of action:
  • This vessel is also equipped with an effective slurry heating system. Heating the slurry is particularly helpful in freeing the high viscosity hydrocarbons from the surface of the slurry solid particles.
  • a second mixing system in which the principal reactions take place, is the tubular reactor in form of one or several tubular units which may work in parallel should the amount of the polluted or industrial material warrant it. This system is: • very effective;
  • the process and equipment in accordance with a preferred embodiment of this invention do not require the bringing of extra hazardous chemicals to the site and do not release hazardous byproducts to the environment.
  • all acidic byproducts such as, CO 2 , SO 3 and HCI will be neutralized by calcium hydroxide or like alkaline reagents.
  • Electric power is necessary to run all the required equipment and processes. In many in-field operations the grid power supply is not available. A conventional independent diesel electric power generator 1 is provided.
  • the Oxidation Gas generator consists of two basic units, a conventional oxygen separator 3 and a conventional ozone generator 4.
  • the source of oxygen is air which may be purified and filtered in air purifier 2.
  • Oxygen is preferably separated by a molecular sieve device.
  • the output oxygen concentration is 90-97% by weight, and the nitrogen concentration is less than 3% - 10% by weight, while other air components are in very small amounts.
  • the air purification unit 2 may be used.
  • To produce oxidation gases a conventional ozone generator is preferably used.
  • the input gas is the oxygen/nitrogen mixture from the oxygen separator 3.
  • the ozone generator may have an output ozone concentration of more than 9% by weight. Oxygen, nitrogen, nitrogen oxides (NO x ), which result from reactions with ozone, and other air components constitute the remaining components of the oxidation gases.
  • Oxidation Gas Supply and Distribution System 5 provides the oxidizing gases and ensures their dispersion into the process stream preferably before the process stream is pressurized and introduced to the tubular reactor.
  • the oxidation gas distribution system may introduce the oxidative gases into the process stream in a variety of ways.
  • the gases under pressure may be introduced upstream of the pump for pressurizing the process stream where the pump effects a dispersion of the gases throughout the power stream.
  • the gases may be injected into the reactor at various intervals.
  • a further alternative includes the use of a water ejector such as a MazzeiTM ejector.
  • the oxidation gases are supplied to the ejector at a minimum pressure of 5 to 20 psi injected straight into suction side of the pump.
  • the water ejector is preferably used because of its economical way of dispersing the gases in the liquid.
  • the ejector's nozzle diameter is adjusted depending on the required volume and pressure of the gases.
  • the water/gas stream enters the pump to increase further the stream's pressure to above 50 psig. Such an increased pressure ensures a better solubility of the Oxidation Gases in the process stream.
  • the water used in this process may be fresh, polluted or recycled from the cleaning or oxidation process.
  • the recycled stream preferably has solid particulate sizes less than 170 microns.
  • inline mixers may be mounted in the tubular reactor.
  • the mixers may be stainless steel metal plates with tabs, slats or the like extending into the flow stream to disrupt flow and generate turbulence in the stream.
  • the degree of gas dispersion depends on the design of the inline mixer and the flow rate of the slurrry, it being appreciated that many well known designs are available.
  • the amount of the dissolved gases depends on pressure and on turbulence intensity and mass transfer and slurry temperature in the tubular reactor.
  • the advantage of this system is that it requires neither a separate bypass pipe nor an extra supply of water or stream free of solid particles. It is inexpensive to design, build and maintain.
  • the selection of a particular system for use in the cleaning or oxidation unit depends on the operational capacity of the unit. For small laboratory and pilot units the water ejector system is preferred, while for a large unit, operating in batch load or continuous load modes, the multipoint introduction system is preferred. This system is also more suitable to treat coarse pollutant particles or oxidative compounds.
  • the tubular reactor 6 is designed to carry out several different types of reactions while cleaning the polluted water solution, emulsion and/or solid slurry and/or carrying out industrial processes. It offers the capability to clean, separate or decompose pollutants of several types, such as hydrocarbons, PCBs, cyanides, heavy metals, etc.
  • the entire system is designed to work as a separate unit in the batch load mode, or as a component of the whole cleaning system working in the continuous load mode.
  • the pretreatment vessel 8 is capable of working in the floatation separation, highly-oxidizing decomposition or adsorption operating modes.
  • the floatation process is applied when a large concentration of hydrocarbons occurs in the polluted water, solid slurry or solids. In this process, the incoming concentration of hydrocarbons is reduced to below 3 to 7%. After the initial floatation cleaning, the final decomposition of the pollutants is done by the oxidation treatment.
  • the oxidation process alone i.e. with no initial floatation cleaning, may only be required when the incoming pollutant concentration is below 7%.
  • the treatment system according to this embodiment comprises four principal units:
  • the floatation process usually require pre-heating of the treated slurry.
  • the necessary temperature is 30-60°C depending on the polluted material composition and viscosity. Consequently, a hot water tank and a heating system 15 with the usual (i.e. propane-butane or diesel oil) burners or electric heating system. Hot water, polluted or recycled from the cleaning or industrial process 16, is supplied to the pretreatment vessel 8 in which the polluted solid material is also added from screening system 7.
  • the pretreatment vessel 8 is a container built preferably of stainless 316S steel and may have two floatation mixing devices inside.
  • the pretreatment vessel has three additional systems:
  • the conical bottom of the pretreatment reactor is supplemented with a specially designed variable drive auger 9.
  • the discharge from the auger is directed via the slurry pump 10 into the tubular reactor 6.
  • Preparation by mixing of water/solid slurry to be cleaned or oxidized • Preferable volume of tubular processor should be 60% to 90% total volume with preferably 80%.
  • process stream contains sufficient amounts of hydrocarbons, separation of hydrocarbons by floatation or adsorption in the pretreat reactor is preferred.
  • separation of hydrocarbons by floatation or adsorption in the pretreat reactor is preferred.
  • the most economical slurry mixing system and mass transfer is provided by the slurry's turbulent flow inside circular pipes. Mixing of this type is used in the tubular reactor 6.
  • This reactor has the following advantageous characteristics over the conventional reactors: low energy consumption; simple to design and construct; fully hermetic; the highest mass and heat transfers between solid, liquid and gaseous reagents; low operational and maintenance cost; no moving parts; easy to adjust in order to attain the required mass transfer; responds readily to changes in its operating parameters; • much more effective than conventional mixing systems; easy to replace; low investment cost; easy to cool or thermal insulate; possible to build within each other; • the tubular reactor from safety point of view may be built with double walls to prevent environmental damage due to the potential of outside wall leakage from the main reactor; • easy to install emergency shutoff valves
  • the tubular reactor 6 may be a device consisting of several extended tube lines or coils working in a parallel or single extended line. Such a system is very flexible and convenient. In particular, it offers the possibility to alter the processor's volume/capacity by switching on/off its different tubular sections, depending on the volume of the material to be processed, sections may be disconnected, if needed for maintenance or upgrading, without impacting the efficiencies of the ongoing cleaning process.
  • the mixing conditions can be adjusted as needed.
  • Another way in which the mixing may be adjusted is to change the flow rate of the slurry.
  • Exemplary process conditions include, for example, in the separation of oxygen from air by a molecular sieve device, the oxygen concentration in the resulting oxidation gas may be about 75% to about 85% by weight, while the concentration of nitrogen and nitrogen oxide components may be about 5% to about 10% by weight and ozone may be about 8% to about 14% by weight and the balance being inert gases
  • the nitrogen oxides play an important catalyst role in the oxidation treatment of pollutants or any industrial oxidation processes.
  • the pressure of the oxidation gases is preferably at a minimum of 5 psig and may be dispersed into the process stream in various ways.
  • the oxidation gases may be dispersed in liquid and/or slurry preferably as very small bubbles, of the diameter less than 0.5 mm, in order to ensure their substantially increased contact surface with the pollutants or industrial oxidizable compound.
  • a water ejector may be used as the most economical way to disperse the Oxidation Gases in the process stream.
  • the ejector's nozzle diameter depends on the volume and pressure of the Oxidation Gases, type and concentration of the pollutant and/or industrial oxidizing process compounds in water and/or water-solid slurry.
  • the Mazzie ejector may be placed on inlet (suction side) of the pump.
  • the ejector may be of the type described in U.S. patent 4,123,800.
  • the diameter and the length of the tubular reactor 6 are selected such, as to produce strong turbulence to ensure high mixing of all three reacting phases: gaseous oxidants, polluted liquids and polluted solids.
  • the selected dimensions of the tubular reactor 6 also depend on liquid/solid pollutant concentration, pollutant amount, pollutant density and solids particle size distribution.
  • the flow rate is adjusted so that at a given diameter of the tubular reactor, and at a given amount of gases and liquid slurry no separation of the gaseous phase occurs and no sedimentation of larger and heavier solid pollutant particles takes place in the tubular processor.
  • the volume of the tubular reactor and recycle rate is selected to preferably provide a residence time of up to 30 minutes and most preferred in the range of about 5 to 10 minutes.
  • the selected specification for the tubular processor, type and size of the slurry pump and slurry flow rate are selected to ensure that the slurry pressure in the tubular processor is 50 - 500 psig and preferably 200 psig, enabling a high solubility of the oxidation gases in liquid and/or slurry to occur.
  • the higher pressures ensure penetration of the oxidizing gases into pores of the materials to be processed.
  • the waste components may be found in porous materials such as rock formations and soil reclamation.
  • the oxidation gases are forced into the pores of the porous process materials to provide a more complete oxidation treatment thereof.
  • the oxidation gases are dispersed in the liquid phase before it enters the high-pressure pump 10 to increase the gas solubility.
  • concentration of oxidation gases introduced into the process stream is in the range of about 0.04% to about 0.1 % by weight.
  • the liquid/gas stream is injected to the tubular reactor 6 containing the polluted slurry and/or industrial compound to be oxidized.
  • the slurry pump preferably has the capability to handle particle sizes up to about 8 cm. and up to about 60 weight % solids in the slurry and up to about 20 weight % of oxidation gases.
  • pH of the treated solution/emulsion and/or slurry has to be adjusted to a desired range of 9 to 14 and most preferably around about 14 This level of pH ensures that sufficient amounts of oxidizing components including free radicals are produced by the oxidation gases.
  • the oxidation gases are dispersed in liquid and/or slurry preferably as very small bubbles, of the diameter less than 0.5 mm, in order to ensure their substantially increased contact surface with the pollutants and/or industrial process compounds.
  • in line mixers mounted in the tubular reactor 6 are used.
  • the mixers are preferably round stainless steel plates of 5-8 mm thickness with radial slits, the triangular parts bent outwardly to form tabs which interfere with the flow patterns.
  • the degree of gas dispersion depends on the number, the size and the shape of the slits.
  • the amount of the gases actually dissolved depends on the pressure and temperature in the tubular reactor and on the intensity of turbulence inside it.
  • a three tier treatment system is provided wherein: • Tier One: Separation of coarse solid particles larger than 80 mm and preferably less than 7 mm prior to supplying them into the pretreatment vessel 8. • Tier Two: The smaller solid particles, which were screened in the pretreatment vessel 8, are suspended in water up to about 60% by weight and pH is adjusted to the range of 8 to 9. Subsequently, this slurry is processed in the Pretreatment vessel by the Oxidation Gases, which are recycled back from the tubular reactor 6. • Tier Three: During the transport of the treated solution and/or slurry from the pretreatment vessel 8 to the reactor 6.
  • the Oxidation mixture i.e., for example, water with Oxidation Gases dissolved and dispersed in it, is injected into the slurry from unit 5.
  • the batch process i.e. one large load of the polluted material
  • partly cleaned slurry and/or industrial process compounds is recycled back to the pretreatment vessel and once it reaches again the tubular reactor 6, a new portion of Oxidation Mixture is delivered from unit 5. The process is repeated until a satisfactory level of oxidation is achieved.
  • injection of the Oxidation Mixture from unit 5 may take place in several entry points to the tubular reactor 6 to obtain the required pollutant decomposition level.
  • the preferred recirculation percentage in the continuous process is in the range of about 60% to 90% of the process stream directed back into the system.
  • the coarse pollutant particles separated in Tier One are washed by a detergent solution or a solvent emulsion suitable for the particular pollutant in the ambient or increased temperature and pressure. Cleaned particles are discharged from the system while the polluted detergent and/or solvent liquid is recycled to the new portion of the polluted coarse material. Once this liquid becomes fully loaded with pollutant it is pumped into the pretreatment vessel 8 as a carrier liquid during the preparation of the fine solid slurry.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Soil Sciences (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne un procédé d'oxydation pouvant s'effectuer par cuvées ou en continu. Ce procédé d'oxydation est efficace pour traiter des substances polluantes dans des flux de déchets, et pour traiter des flux contenant du minerai à des fins de récupération d'or ou analogue. Le procédé consiste à placer le flux au contact de gaz d'oxydation contenant de l'ozone. Le flux de traitement est ensuite pompé sous pression vers un réacteur tubulaire étendu pour obtenir un degré d'oxydation des matériaux désiré dans le flux de traitement pendant que la pression est maintenue dans le réacteur tubulaire. Le flux sous pression augmente la solubilité des gaz d'oxydation dans le flux de traitement, et la pénétration des gaz d'oxydation dans les pores du flux de traitement est contrôlée et maintenue pour assurer la production de radicaux libres oxydants et pour neutraliser tout acidité libérée dans le réacteur tubulaire. La température du flux de traitement est contrôlée et réglée de manière à optimiser l'oxydation, la solubilité des gaz d'oxydation et la dégradation de l'ozone.
PCT/CA2001/000261 2000-03-03 2001-03-02 Procede et appareil pour realiser des traitements par oxydation tres efficaces WO2001064587A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2001239044A AU2001239044A1 (en) 2000-03-03 2001-03-02 Method and unit for achieving highly effective oxidation treatments

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US18667100P 2000-03-03 2000-03-03
US60/186,671 2000-03-03

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WO2001064587A2 true WO2001064587A2 (fr) 2001-09-07
WO2001064587A3 WO2001064587A3 (fr) 2001-12-13

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107716516A (zh) * 2017-10-31 2018-02-23 长春黄金研究院 一种氰化尾渣的氰化物去除方法

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US4619763A (en) * 1983-07-21 1986-10-28 Brien Edward J O Ozone H2 O treatment
EP0261822A2 (fr) * 1986-09-18 1988-03-30 The BOC Group plc Traitement de déchets aqueux
US4751005A (en) * 1986-08-22 1988-06-14 Nippon Shokubai Kagaku Kogyo Co., Ltd. Method for treatment of waste water
EP0461385A1 (fr) * 1990-06-08 1991-12-18 Krupp Koppers GmbH Procédé de traitement des eaux usées provenant d'une installation de gazéification travaillant sous haute pression
EP0478528A1 (fr) * 1990-09-27 1992-04-01 Kamyr, Inc. Procédé et appareil pour le traitement d'eaux usées
WO1993008935A1 (fr) * 1991-10-31 1993-05-13 Bernd Heim Procede et dispositif de traitement de dechets broyables contenant du liquide
WO1995005346A1 (fr) * 1993-08-18 1995-02-23 Gilboy John P Jr Procede d'epuration a l'ozone de liquides contamines
WO1996021623A1 (fr) * 1995-01-10 1996-07-18 Coury William S Systeme de reacteur de decontamination et son mode d'utilisation
US5547584A (en) * 1994-03-17 1996-08-20 Electronic Drilling Control, Inc. Transportable, self-contained water purification system and method
WO1998012003A1 (fr) * 1996-09-19 1998-03-26 The Boc Group Plc Traitement des dechets
DE19909160A1 (de) * 1999-03-03 2000-09-07 Philaqua Aufbereitungstechnik Ozonung von Schlämmen und Schlick und dickflüssigen Medien zur Entgiftung von toxischen Substanzen

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3772188A (en) * 1972-02-28 1973-11-13 R Edwards Sewage treatment apparatus and method
US4619763A (en) * 1983-07-21 1986-10-28 Brien Edward J O Ozone H2 O treatment
US4751005A (en) * 1986-08-22 1988-06-14 Nippon Shokubai Kagaku Kogyo Co., Ltd. Method for treatment of waste water
EP0261822A2 (fr) * 1986-09-18 1988-03-30 The BOC Group plc Traitement de déchets aqueux
EP0461385A1 (fr) * 1990-06-08 1991-12-18 Krupp Koppers GmbH Procédé de traitement des eaux usées provenant d'une installation de gazéification travaillant sous haute pression
EP0478528A1 (fr) * 1990-09-27 1992-04-01 Kamyr, Inc. Procédé et appareil pour le traitement d'eaux usées
WO1993008935A1 (fr) * 1991-10-31 1993-05-13 Bernd Heim Procede et dispositif de traitement de dechets broyables contenant du liquide
WO1995005346A1 (fr) * 1993-08-18 1995-02-23 Gilboy John P Jr Procede d'epuration a l'ozone de liquides contamines
US5547584A (en) * 1994-03-17 1996-08-20 Electronic Drilling Control, Inc. Transportable, self-contained water purification system and method
WO1996021623A1 (fr) * 1995-01-10 1996-07-18 Coury William S Systeme de reacteur de decontamination et son mode d'utilisation
WO1998012003A1 (fr) * 1996-09-19 1998-03-26 The Boc Group Plc Traitement des dechets
DE19909160A1 (de) * 1999-03-03 2000-09-07 Philaqua Aufbereitungstechnik Ozonung von Schlämmen und Schlick und dickflüssigen Medien zur Entgiftung von toxischen Substanzen

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Publication number Priority date Publication date Assignee Title
CN107716516A (zh) * 2017-10-31 2018-02-23 长春黄金研究院 一种氰化尾渣的氰化物去除方法

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