WO1993025481A1 - Process and apparatus for purifying streams - Google Patents

Process and apparatus for purifying streams Download PDF

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Publication number
WO1993025481A1
WO1993025481A1 PCT/NL1993/000119 NL9300119W WO9325481A1 WO 1993025481 A1 WO1993025481 A1 WO 1993025481A1 NL 9300119 W NL9300119 W NL 9300119W WO 9325481 A1 WO9325481 A1 WO 9325481A1
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WIPO (PCT)
Prior art keywords
packed bed
ozone
activated carbon
process according
cod
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Ceased
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PCT/NL1993/000119
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French (fr)
Inventor
Jan Peter Campen
Blandikus Catharikus Jaspers
Joannes Petrus Kaptijn
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ECO Purification Systems BV
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ECO Purification Systems BV
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Publication date
Priority to DE69304699T priority Critical patent/DE69304699T2/en
Priority to EP93916271A priority patent/EP0643674B1/en
Priority to RU9294046244A priority patent/RU2088538C1/en
Priority to MD96-0247A priority patent/MD960247A/en
Priority to JP6501343A priority patent/JP2748047B2/en
Priority to SK1477-94A priority patent/SK147794A3/en
Priority to RO94-01921A priority patent/RO113028B1/en
Priority to US08/338,491 priority patent/US5565107A/en
Priority to AU45877/93A priority patent/AU668747B2/en
Application filed by ECO Purification Systems BV filed Critical ECO Purification Systems BV
Priority to BR9306478A priority patent/BR9306478A/en
Publication of WO1993025481A1 publication Critical patent/WO1993025481A1/en
Priority to NO944657A priority patent/NO944657L/en
Priority to FI945689A priority patent/FI945689A0/en
Anticipated expiration legal-status Critical
Priority to TJ96000349A priority patent/TJ190R3/en
Priority to GR960402718T priority patent/GR3021345T3/en
Priority to HK134397A priority patent/HK134397A/en
Ceased legal-status Critical Current

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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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46109—Electrodes
    • C02F1/46114—Electrodes in particulate form or with conductive and/or non conductive particles between them
    • 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

Definitions

  • the invention relates to a process for purifying streams which contain organic and/or inorganic impurities, the stream to be treated being introduced into a water-containing reaction zone, and to an apparatus which can be used for this process.
  • Dutch Patent Application 9000118 discloses a method for purifying streams which contain organic and/or inorganic impurities, in which the stream to be treated is introduced into a water-containing reaction zone to which current is supplied via one or more electrodes while a substance is supplied at the same time which, under the influence of the electric current supplied, produces radicals which react with the impurities.
  • substances of this type comprise methane, carbon monoxide, hydrogen, ammonia, oxygen, ozone and hydrogen peroxide.
  • the substance producing electrochemical radicals in the process is preferably fed to the reaction zone via a porous electrode.
  • the residence time in the reaction zone can be shortened by employing elevated temperatures, preferably in the range from 10 to 95 C. The degree of conversion and the electric energy consumption in this known method still leaves something to be desired.
  • a process and apparatus for electrochemical reactions to be used for pollution control are known from US-A-3,915,822.
  • An electrochemical cell is used wherein an electrolyte - which contains impurities or undesirable components - is treated in a reaction zone containing electrically conductive particles, e.g. carbon pellets, as well as a plurality of electrodes.
  • the conductive particles may consist of activated carbon in granular, spherical or other form.
  • the voltage is normally a DC potential gradient in the order of 0.1 to 10 Volts/cm.
  • a gas reactant such as O 3 or Cl 2 may be used.
  • a mixture of O 3 in a diluent gas can be introduced to the liquid filled bed of electrically conductive particles as fine bubbles containing ozone in an amount of 2-20 vol .% .
  • the use of a sub-stoichiometrie amount of ozone or any other reactant is not suggested.
  • the object of the present invention is to overcome the above-mentioned drawbacks regarding energy consumption and expensive starting materials.
  • the invention provides a process for purifying streams which contain undesirable organic and/or inorganic impurities which impurities may be converted into harmless compounds by reduction or oxidation, the stream to be treated being introduced into a water-containing reaction zone which comprises a packed bed of activated carbon to which an electrochemical potential is applied and to which ozone or hydrogen is fed at the same time.
  • COD Cemical Oxygen Demand
  • a theoretical Chemical Hydrogen Demand can be defined (for reducible impurities), i.e. the amount of hydrogen necessary for a complete reduction with hydrogen of the micro pollutants present in the waste water.
  • CHD Chemical Hydrogen Demand
  • the process according to the invention gives rise to a lower ozone consumption than mentioned above, that is sub-stoechiometric of less than 1 kilogram of ozone per kilogram of COD reduced. The same is valid for the hydrogen consumption and CHD degradation. Consequently, the process according to the invention is characterised in that a reactant selected from ozone and hydrogen is, at the same time, fed into the reaction zone in a sub-stoechiometric amount.
  • the residence time in the reactor is low, i.e. considerably more advantageous than the effects according to WO 90/14312 and NL 9000118. It is a matter of a synergistic effect, as said effects are more favourable than the sum of the effects obtained in using the process according to said two literature references. This has been shown on the basis of experiments which will be described hereinafter.
  • a reaction zone is preferably used in which the packed bed of activated carbon consists of particles having a surface of at least 50 m 2 /g, preferably 200-1200 m 2 /g and a pore volume of at least 0.05 cm 3 /g, preferably 0.1-0.3 cm 3 /g.
  • an embodiment is used according to the invention in which the electrochemical potential of the packed bed is less than 10 volts with respect to an Hg/HgSO 4 reference electrode and preferably is in the range of 0.1-4 volts.
  • the value of the electrochemical potential is less than the voltage required for the electrolysis of water, i.e. the quantitative electrolysis of water using the cell configuration in question.
  • the potential at which water electrolysis occurs depends on the electrode material and is therefore always different for each reactor. Carbon electrodes have a relatively high overpotential for the generation of hydrogen. Furthermore, if the electrode material is contaminated, it is possible for water electrolysis to occur to a slight extent even at lower potentials. Many opposing reactions exist, but the K and Na ions which are present, for example, will not be deposited as a metal on the counterelectrode but give rise to generation of hydrogen and formation of OH-. The deposition of heavy metals, on the other hand, is possible.
  • the ozone or hydrogen consumption is surprisingly low.
  • ozone is used in an amount of 0.001-0.5 kg O 3 /kg COD of the impurities to be removed, preferably 0.005-0.3 kg O 3 /kg COD and/or in which hydrogen is used in an amount of 0.001-0.5 kg H 2 /kg CHD of the impurities to be removed, preferably 0.005-0.3 kg H 2 /kg CHD.
  • the process according to the invention therefore involves a substoichiometric ozone consumption.
  • the process according to the invention is based on a totally different mechanism compared to conventional oxidations with ozone. Thanks to this special mechanism, the process according to the invention is also suitable for the oxidation substances which cannot readily be decomposed, such as chlorinated hydrocarbons, for example freons. In the latter case carbonates, chlorides and/or fluorides are produced. Ammonia can be decomposed to give the harmless nitrogen gas.
  • the process according to the invention preferably employs a temperature in the reaction zone of at least 20°C, preferably 30-80°C. This is remarkable because, in the case of the conventional decomposition processes using ozone, there is the effect of the considerably reduced solubility of ozone gas in water at elevated temperature. In the conventional processes, therefore, an elevated pressure is used preferably (in order to accelerate the decomposition processes), which has the effect of increasing the cost of the installation. In the process according to the invention, the use of elevated pressure is unnecessary or necessary only to a small degree.
  • the invention also relates to an apparatus suitable for carrying out the process described above.
  • This apparatus comprises at least a reaction vessel containing a packed bed of activated carbon which can be operated as an electrode, a contact electrode placed in the packed bed, for the supply or removal of an electric current, a counterelectrode disposed in the reaction vessel, means for electronically insulating the packed bed of activated carbon and the counterelectrode, means for feeding in liquid, means for discharging liquid, means for feeding in ozone-containing gas, means for discharging waste gas.
  • Said means for electronic insulation may be perforated tubes or semipermeable membranes.
  • the electrodes are preferably arranged so as to be detachable, so that any deposits, for example of metals, can be removed therefrom.
  • reference electrode Hg/HgSO 4 via Luggin capillary at liquid inlet
  • waste water type A contains, inter alia: petroleum sulphonates, oleic acids and carbonates.
  • waste water type B contains, inter alia: epichlorohydrin derivatives, allyl chloride derivatives and chloride ions.
  • Type A shows fluctuations because of the varying composition and pH of the incoming liquid.
  • Both the hydrogen consumption and the consumption of electrical charge are less than the expected stoechiometric amounts of 1 g H 2 /g CHD and 26.8 kAh/kg CHD.

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  • Chemical & Material Sciences (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)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Water Treatment By Sorption (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Physical Water Treatments (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Cleaning By Liquid Or Steam (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Treatment Of Water By Ion Exchange (AREA)

Abstract

The invention relates to a process for purifying streams which contain organic and/or inorganic impurities, the stream to be treated being introduced into a water-containing reaction zone which comprises a packed bed of activated carbon to which an electrochemical potential is applied and to which ozone or hydrogen is fed at the same time, and to an apparatus for carrying out said process comprising at least: a reaction vessel containing a packed bed of activated carbon which can be operated as an electrode, a contact electrode, placed in the packed bed, for the supply or removal of an electric current, a counterelectrode disposed in the reaction vessel, means for electronically insulating the packed bed of activated carbon and the counterelectrode, means for feeding in liquid, means for discharging liquid, means for feeding in ozone-containing gas, means for discharging waste gas.

Description

Process and apparatus for purifying streams.
The invention relates to a process for purifying streams which contain organic and/or inorganic impurities, the stream to be treated being introduced into a water-containing reaction zone, and to an apparatus which can be used for this process.
International Patent Application PCT/NL90/00075 (publication number WO 90/14312) discloses a process for the treatment of water which is contaminated with unwanted constituents such as (aromatic)
hydrocarbons and pesticides, by treating the contaminated water or the gaseous and/or liquid components present therein or originating therefrom with ozone and a catalyst such as activated carbon, the catalyst being regenerated continuously with ozone. This process, however, has the drawback that the ozone consumption for the purpose of decomposition of the impurities (expressed as COD = chemical oxygen demand), in spite of the relatively low values, is still too high for many applications and the residence time in the reactor is rather long.
Dutch Patent Application 9000118 discloses a method for purifying streams which contain organic and/or inorganic impurities, in which the stream to be treated is introduced into a water-containing reaction zone to which current is supplied via one or more electrodes while a substance is supplied at the same time which, under the influence of the electric current supplied, produces radicals which react with the impurities. The examples given of substances of this type comprise methane, carbon monoxide, hydrogen, ammonia, oxygen, ozone and hydrogen peroxide. The substance producing electrochemical radicals in the process is preferably fed to the reaction zone via a porous electrode. The residence time in the reaction zone can be shortened by employing elevated temperatures, preferably in the range from 10 to 95 C. The degree of conversion and the electric energy consumption in this known method still leaves something to be desired.
A process and apparatus for electrochemical reactions to be used for pollution control are known from US-A-3,915,822. An electrochemical cell is used wherein an electrolyte - which contains impurities or undesirable components - is treated in a reaction zone containing electrically conductive particles, e.g. carbon pellets, as well as a plurality of electrodes. The conductive particles may consist of activated carbon in granular, spherical or other form. The voltage is normally a DC potential gradient in the order of 0.1 to 10 Volts/cm. During the process of this US patent a gas reactant such as O3 or Cl2 may be used. It is indicated that a mixture of O3 in a diluent gas can be introduced to the liquid filled bed of electrically conductive particles as fine bubbles containing ozone in an amount of 2-20 vol .% . The use of a sub-stoichiometrie amount of ozone or any other reactant is not suggested.
The object of the present invention is to overcome the above-mentioned drawbacks regarding energy consumption and expensive starting materials.
To this end, the invention provides a process for purifying streams which contain undesirable organic and/or inorganic impurities which impurities may be converted into harmless compounds by reduction or oxidation, the stream to be treated being introduced into a water-containing reaction zone which comprises a packed bed of activated carbon to which an electrochemical potential is applied and to which ozone or hydrogen is fed at the same time.
The degree of polution for oxidisable impurities can be quantified as Cemical Oxygen Demand (COD). This relates to the standard USEPA method of analysis which determines the amount of oxygen that would be needed for a near complete oxidation of the micro pollutants. Evidently, in ozonation processes the resulting reaction products are also formed by introduction of oxygen into the molecules of the micro pollutants.
Obeying the law of mass conservation one would expect to find an equal mass of ozone consumed as the mass of COD reduced if all oxygen atoms of the ozone molecule would have been effectively used. Sub-stoechiometry in ozone is present if lower values than 1 kg O3 / kg COD are found.
Analogous to the COD a theoretical Chemical Hydrogen Demand (CHD) can be defined (for reducible impurities), i.e. the amount of hydrogen necessary for a complete reduction with hydrogen of the micro pollutants present in the waste water. For instance, the nitrate reduction using a Pd/Cu catalyst (Th. Tacke et al., Dechema-Monographie
Katalyse, 122, 15-27, Frankfurt/M 1991) gives the reaction: 2NO-3 + 5H2 → N2 + 4H2O + 2OH- at elevated pressure. Using both the molar weights of the nitrate and the hydrogen for e.g. a 100 mg nitrate per litre solution the CHD amounts 8.06 mg H2/l. Similarly sub-stoechiometry in hydrogen arises when a lower hydrogen consumption is found than 1 kg H2 / kg CHD.
Surprisingly the process according to the invention gives rise to a lower ozone consumption than mentioned above, that is sub-stoechiometric of less than 1 kilogram of ozone per kilogram of COD reduced. The same is valid for the hydrogen consumption and CHD degradation. Consequently, the process according to the invention is characterised in that a reactant selected from ozone and hydrogen is, at the same time, fed into the reaction zone in a sub-stoechiometric amount.
The residence time in the reactor is low, i.e. considerably more advantageous than the effects according to WO 90/14312 and NL 9000118. It is a matter of a synergistic effect, as said effects are more favourable than the sum of the effects obtained in using the process according to said two literature references. This has been shown on the basis of experiments which will be described hereinafter.
In the process according to the invention, a reaction zone is preferably used in which the packed bed of activated carbon consists of particles having a surface of at least 50 m2/g, preferably 200-1200 m2/g and a pore volume of at least 0.05 cm3/g, preferably 0.1-0.3 cm3/g.
In general, an embodiment is used according to the invention in which the electrochemical potential of the packed bed is less than 10 volts with respect to an Hg/HgSO4 reference electrode and preferably is in the range of 0.1-4 volts. In particular, the value of the electrochemical potential is less than the voltage required for the electrolysis of water, i.e. the quantitative electrolysis of water using the cell configuration in question.
The potential at which water electrolysis occurs depends on the electrode material and is therefore always different for each reactor. Carbon electrodes have a relatively high overpotential for the generation of hydrogen. Furthermore, if the electrode material is contaminated, it is possible for water electrolysis to occur to a slight extent even at lower potentials. Many opposing reactions exist, but the K and Na ions which are present, for example, will not be deposited as a metal on the counterelectrode but give rise to generation of hydrogen and formation of OH-. The deposition of heavy metals, on the other hand, is possible.
The consumption of electrical charge is lower than expected. In case of conventional Faradayan electrochemical oxidation one would expect that for each oxygen atom introduced in the micro pollutant molecule two electrons would be needed. The number of oxygen atoms introduced is again directly dependent on the lowering of COD content of the effluent. In general the theoretical specific electric consumption equals:
(n * F)/(3600 * M) in kAh/kg reduced (or n * F Coulombs per mole), with n the number of electrons involved, F the Faraday constant and M the molar weight of the micro pollutant, oxygen in case of COD or hydrogen in case of CHD. So, if per kilogram of COD reduced, less thans 3-35 kAh is introduced sub=stoechiometry in electrical charge is present. Sustantially lower electrical currents are necessary than theoretically expected based on the conversions as mentioned in the table hereafter. A similar reasoning applies for the CHD. This results in an amount of charge of less than 26.8 kAh/kg CHD. Consequently, it is preferred in the process of the invention that the used amount of charge is less than 3-35 kAh/kg COD in case of oxidation with O3 or less than 26.8 kAh/kg CHD in case of reduction with H2.
In the process according to the invention, the ozone or hydrogen consumption is surprisingly low. In an embodiment of the invention ozone is used in an amount of 0.001-0.5 kg O3/kg COD of the impurities to be removed, preferably 0.005-0.3 kg O3/kg COD and/or in which hydrogen is used in an amount of 0.001-0.5 kg H2/kg CHD of the impurities to be removed, preferably 0.005-0.3 kg H2/kg CHD.
The process according to the invention therefore involves a substoichiometric ozone consumption. This indicates that the process according to the invention is based on a totally different mechanism compared to conventional oxidations with ozone. Thanks to this special mechanism, the process according to the invention is also suitable for the oxidation substances which cannot readily be decomposed, such as chlorinated hydrocarbons, for example freons. In the latter case carbonates, chlorides and/or fluorides are produced. Ammonia can be decomposed to give the harmless nitrogen gas.
Using the process according to the invention, it is possible to employ, apart from the oxidations with ozone, reduction reactions with hydrogen to good effect. Thus it is possible, for example, to convert nitrate dissolved in water into nitrogen gas, if hydrogen gas is fed in in the process according to the invention.
Employing a higher temperature than room temperature in general produces a further improvement of the abovementioned effects. Therefore, the process according to the invention preferably employs a temperature in the reaction zone of at least 20°C, preferably 30-80°C. This is remarkable because, in the case of the conventional decomposition processes using ozone, there is the effect of the considerably reduced solubility of ozone gas in water at elevated temperature. In the conventional processes, therefore, an elevated pressure is used preferably (in order to accelerate the decomposition processes), which has the effect of increasing the cost of the installation. In the process according to the invention, the use of elevated pressure is unnecessary or necessary only to a small degree.
The invention also relates to an apparatus suitable for carrying out the process described above. This apparatus comprises at least a reaction vessel containing a packed bed of activated carbon which can be operated as an electrode, a contact electrode placed in the packed bed, for the supply or removal of an electric current, a counterelectrode disposed in the reaction vessel, means for electronically insulating the packed bed of activated carbon and the counterelectrode, means for feeding in liquid, means for discharging liquid, means for feeding in ozone-containing gas, means for discharging waste gas. Said means for electronic insulation may be perforated tubes or semipermeable membranes.
In the apparatus according to the invention, the electrodes are preferably arranged so as to be detachable, so that any deposits, for example of metals, can be removed therefrom.
An embodiment of the apparatus according to the invention is depicted in the figure. The symbols in this figure have the following meaning:
1 reaction vessel,
2 packed bed of activated carbon,
3 contact electrode placed in the packed bed,
4 perforated electrode screen for electronically insulating the packed bed of activated carbon and the counterelectrode,
5 counterelectrode,
6 diffusor for gas input (which ensures a good distribution of the feed gas over the entire bed of activated carbon),
7 inlet for ozone- or hydrogen-containing gas,
8 inlet for (contaminated) liquid,
9 discharge for treated liquid,
10 discharge for waste gas.
The invention is explained on the basis of experiments.
These experiments made use of a glass reactor. This is provided with a gas diffuser at the bottom and a perforated PVC inner tube in the centre. In this tube, a graphite counterelectrode is positioned, and around the tube there is a bed of activated carbon. In addition, a graphite tube is placed in the bed as a current collector. The following data are of interest: Reactor:
length = 1 meter
internal diameter = 5 cm
liquid flow rate = 16-20 ml/min
gas flow rate = 200-300 ml/min
liquid volume = 400 ml
Activated carbon:
bulk density = 380 g/l
grain diameter = 0.8 mm
total pore volume = 1.0 cm3/g
specific surface = 1000-1200 m2/g
iodine adsorption = 1050 mg/g
weight = 700 g
Counterelectrode:
material = carbon
length = 1.2 meters
diameter = 1.0 cm
Perforated tube:
Material = PVC
length = 1.2 meter
diameter = 1.3 cm
Potentiostat/reference:
trademark = Bank
type = HP-88
reference electrode = Hg/HgSO4 via Luggin capillary at liquid inlet
current = 0.085-0.200 A
Current density = 2.6 - 6.1 10-4 A/cm2 max (decreasing in the radial direction) The results of the tests are summarised in Table A.
TABLE A
Waste Residence Ozone Voltage Sp.Electr. Electr. CODIN CODOUT Conwater time consumption vs. ref. Consumption Consumption version type* [minutes] [gOs/gCOD] [volts] [kAh/kgCOD] [kWh/kgCOD] [mg/l] [mg/l] %
A 20 0.25 2.50 0.023 0.09 4300 1100 74
25 0.30 2.50 0.026 0.10 4300 883 79
B 24 0.024 2.50 0.0033 0.013 71000 12400 83
24 0.048 2.50 0.0029 0.011 71000 20000 72
*) waste water type A contains, inter alia: petroleum sulphonates, oleic acids and carbonates.
*) waste water type B contains, inter alia: epichlorohydrin derivatives, allyl chloride derivatives and chloride ions.
Using a comparable treatment according to the process of WO 90/14312, results are achieved which are summarised in Table B.
TABLE B
Waste water Residence Ozone Voltage Electr. CODIN CODOUT Contype time consumption vs. ref. Consumption version
[minutes] [gO3/gCOD] [volts] [kWh/kg COD] [mg/l] [mg/l] %
A 58 5.6 0 0 3700* 3255 12
58 2.5 0 0 3700* 2935 21
B 81 3.9 0 0 54260 16881 69
133 5.3 0 0 54260 13310 75 failed to accomplish higher conversions
Type A shows fluctuations because of the varying composition and pH of the incoming liquid.
This conventional process fails because of a still excessive COD value and in absolute terms it consumes an extraordinarily large amount of ozone, given the high COD contents. Using a comparable treatment according to the process of NL 9000118, results are achieved which are summarised in Table C.
TABLE C
Waste water residence Ozone Voltage Electr. COD IN COD OUT Contype time consumption vs. ref. Consumption version
[minutes] [gO3/gCOD] [volts] [kWh/kg COD] [mg/l] [mg/l] % A 120 0 - 7580
B 60 0 1.8 0.19 61000 35000 43
120 0 1.8 0.42 61000 36000 41 failed to accomplish higher conversions
Again the degradation of COD comes to a standstill at high COD levels so no higher conversion were possible using this system.
The process according to the invention is also applied for reduction of nitrate in water. The results are stated in table D.
Tabel D
Residence Hydrogen Voltage Sp.Electr. Electr. cNO3- In cNO3- out Contime consumption vs. ref. consumption consumption version
[minutes] [gN2/gCHD] [volts] [kAh/kg CHD] [kWh/kg CHD] [mg/l] [mg/l] %
84 0.59 4 4.44 20.0 886 257 71
84 0.66 4 5.03 22.6 886 319 64
Both the hydrogen consumption and the consumption of electrical charge are less than the expected stoechiometric amounts of 1 g H2/g CHD and 26.8 kAh/kg CHD.

Claims

1. Process for purifying streams which contain organic and/or inorganic impurities, the stream to be treated being introduced into a water-containing reaction zone which comprises a packed bed of activated carbon to which an electrochemical potential is applied and to which, at the same time, a reactant selected from ozone and hydrogen is fed in a sub-stoechiometric amount.
2. Process according to Claim 1, in which the packed bed of activated carbon consists of particles having a surface of at least 50 m2/g, preferably 200-1200 m2/g and a pore volume of at least 0.05 cm3/g, preferably 0.1-0.3 cm3/g.
3. Process according to Claim 1 or 2, in which the electrochemical potential of the packed bed is less than 10 volts with respect to an Hg/HgSO4 reference electrode and preferably is in the range of 0.1-4 volts.
4. Process according to Claim 3. in which the value of the electrochemical potential of the packed bed is less than the voltage required for the electrolysis of water.
5. Process according to any of the preceding claims, wherein the used amount of charge is less than 3-35 kAh/kg COD in case of oxidation with O3 or less than 26.8 kAh/kg CHD in case of reduction with H2.
6. Process according to any of the preceding claims, in which ozone is used in an amount of 0.001-0.5 kg O3/kg COD of the impurities to be removed, preferably 0.005-0.3 kg O3/kg COD and/or in which hydrogen is used in an amount of 0.001-0.5 kg H2/kg CHD of the impurities to be removed, preferably 0.005-0.3 kg H2/kg CHD.
7. Process according to any of the preceding claims, in which a temperature is employed in the reaction zone of at least 20ºC, preferably
30-80°C.
8. Apparatus comprising at least
a reaction vessel containing a packed bed of activated carbon which can be operated as an electrode,
a contact electrode, placed in the packed bed, for the supply or removal of an electric current,
a counterelectrode disposed in the reaction vessel,
means for electronically insulating the packed bed of activated carbon and the counterelectrode,
means for feeding in liquid,
means for discharging liquid, means for feeding in ozone-containing gas,
means for discharging waste gas.
9. Apparatus according to Claim 8, wherein the contact electrode and/or the counterelectrode are arranged so as to be detachable.
****
PCT/NL1993/000119 1992-06-04 1993-06-04 Process and apparatus for purifying streams Ceased WO1993025481A1 (en)

Priority Applications (15)

Application Number Priority Date Filing Date Title
AU45877/93A AU668747B2 (en) 1992-06-04 1993-06-04 Process and apparatus for purifying streams
RU9294046244A RU2088538C1 (en) 1992-06-04 1993-06-04 Method of cleaning stream
BR9306478A BR9306478A (en) 1992-06-04 1993-06-04 Process and apparatus for purifying liquid streams
JP6501343A JP2748047B2 (en) 1992-06-04 1993-06-04 Methods for purifying water streams
SK1477-94A SK147794A3 (en) 1992-06-04 1993-06-04 Process and apparatus for purifying streams
RO94-01921A RO113028B1 (en) 1992-06-04 1993-06-04 PROCEDURE AND DEVICE FOR PURIFYING LIQUID CURVES
US08/338,491 US5565107A (en) 1992-06-04 1993-06-04 Process and apparatus for purifying streams
DE69304699T DE69304699T2 (en) 1992-06-04 1993-06-04 METHOD FOR WATER PURIFICATION
MD96-0247A MD960247A (en) 1992-06-04 1993-06-04 Process and apparatus for purifying streams
EP93916271A EP0643674B1 (en) 1992-06-04 1993-06-04 Process for purifying streams
NO944657A NO944657L (en) 1992-06-04 1994-12-02 Method and apparatus for cleaning rivers
FI945689A FI945689A0 (en) 1992-06-04 1994-12-02 Method and apparatus for purifying flows
TJ96000349A TJ190R3 (en) 1992-06-04 1996-07-10 Process for purifying streams which contain organic and/or inorganic imputities
GR960402718T GR3021345T3 (en) 1992-06-04 1996-10-16 Process and apparatus for purifying streams.
HK134397A HK134397A (en) 1992-06-04 1997-06-26 Process for purifying streams

Applications Claiming Priority (3)

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NL9200989 1992-06-04
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DE19911875A1 (en) * 1999-03-17 2000-09-28 Judo Wasseraufbereitung Device for the electrolytic treatment of water or aqueous solutions
WO2004069754A1 (en) * 2003-02-10 2004-08-19 Nt Nitto Sangyo Co., Ltd Method of decomposing hardly decomposable organic compound and apparatus therefor

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CZ297103B6 (en) 2004-10-06 2006-09-13 Lysytchuk@Oleg Method for purifying fluids by making use of ionized aeration
US7967967B2 (en) * 2007-01-16 2011-06-28 Tesla Laboratories, LLC Apparatus and method for electrochemical modification of liquid streams
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WO2000048945A1 (en) * 1999-02-19 2000-08-24 Winfried Schellbach Device for the electrocatalytic treatment of liquids containing contaminants and/or micro-organisms
DE19911875A1 (en) * 1999-03-17 2000-09-28 Judo Wasseraufbereitung Device for the electrolytic treatment of water or aqueous solutions
WO2004069754A1 (en) * 2003-02-10 2004-08-19 Nt Nitto Sangyo Co., Ltd Method of decomposing hardly decomposable organic compound and apparatus therefor

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ATE142607T1 (en) 1996-09-15
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BR9306478A (en) 1998-01-13
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US5565107A (en) 1996-10-15
NO944657L (en) 1994-12-02
CA2136869A1 (en) 1993-12-23
FI945689A7 (en) 1994-12-02
GR3021345T3 (en) 1997-01-31
TJ190R3 (en) 1998-10-28
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CZ303394A3 (en) 1995-03-15
EP0643674B1 (en) 1996-09-11

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