CA1289334C - Process for destroying organic products with toxic effects and equipment for implementing this process - Google Patents
Process for destroying organic products with toxic effects and equipment for implementing this processInfo
- Publication number
- CA1289334C CA1289334C CA000521262A CA521262A CA1289334C CA 1289334 C CA1289334 C CA 1289334C CA 000521262 A CA000521262 A CA 000521262A CA 521262 A CA521262 A CA 521262A CA 1289334 C CA1289334 C CA 1289334C
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- Prior art keywords
- process according
- hydrogen
- gas
- vapo
- products
- Prior art date
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- Expired - Lifetime
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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
- A62D3/20—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by hydropyrolysis or destructive steam gasification, e.g. using water and heat or supercritical water, to effect chemical change
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
-
- 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
-
- 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
-
- 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
- A62D2203/00—Aspects of processes for making harmful chemical substances harmless, or less harmful, by effecting chemical change in the substances
- A62D2203/10—Apparatus specially adapted for treating harmful chemical agents; Details thereof
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Toxicology (AREA)
- Thermal Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Physics & Mathematics (AREA)
- Business, Economics & Management (AREA)
- Emergency Management (AREA)
- Engineering & Computer Science (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Fire-Extinguishing Compositions (AREA)
- Processing Of Solid Wastes (AREA)
- Treatment And Processing Of Natural Fur Or Leather (AREA)
- Treatments Of Macromolecular Shaped Articles (AREA)
- Food Preservation Except Freezing, Refrigeration, And Drying (AREA)
- Chemical And Physical Treatments For Wood And The Like (AREA)
- Agricultural Chemicals And Associated Chemicals (AREA)
Abstract
"Process for destroying halogenated organic products and equipment for carrying out this process".
Abstract This process is characterized in that it comprises as its main stage a vapo-cracking operation.
The equipment for carrying out this process comprises a combustion and mixing chamber with admission of hydrogen, oxygen and water vapour; at least one reactor to receive the mixture coming from the combustion chamber and the product to be treated and, at the exit from this reactor, stations for condensing, neutralizing and treating the gases.
(See single Figure).
Abstract This process is characterized in that it comprises as its main stage a vapo-cracking operation.
The equipment for carrying out this process comprises a combustion and mixing chamber with admission of hydrogen, oxygen and water vapour; at least one reactor to receive the mixture coming from the combustion chamber and the product to be treated and, at the exit from this reactor, stations for condensing, neutralizing and treating the gases.
(See single Figure).
Description
3~
l The present lnventlon relates to a process for destroylng organlc products wlth toxlc effects, preventlng pollutlon of the environment after an lncldent, accldent or any other case requlrlng these products to be deactlvated.
The inventlon also relates to the equlpment for carrying out thls process.
Xore preclsely, use ls currently belng made, ln certaln flelds of lndustry, of organlc compounds of, for example, the polychloroblphenyl type (usually called PCB> on account of thelr favourable characterlstlcs, especlally thelr good thermal stablllty, thelr good cbemlcal lnertness hnd thelr hlgh dlelectrlc constant 9 Justifylng thelr lntenslve use ln partlcular as flulds for transformers and/or condensers.
However, for some years studles have shown that such products are not blodegradable and that there ls evldence of thelr conslderable accumulatlon ln the food chaln. Furthermore, these studles h~ve shown that these products are hlghly toxlc and exhlbit behavlour whlch may be carclnogenlc~ In vlew of thls research, the governments of varlou~ countries concerned have lssued regulatlons rel~tlng to the use, stor~ge and destruction of these products. The result has been that varlous lndustrlal processes have been developed since then.
These processes generally lnvolve an o~eration of lnclneration wlth an excess of ~lr or oxygen ln devlces such ~s cement furn~ces or domestlc waste lnclner~tors.
Thus, one can clte:
'~ ~
' ~'' , :
~ . .
l - French Patent ~o. 2 323 432 for a c~talytlc decomposltion process of halo~enated organlc compounds;
- Pntent W0 82/0~509 for a decomposltlon process uslng a plasma burner operatlng at between 3000 and 4000 C;
- Patent W0 80~022116 for a decomposltion process uslng a fused salt and an oxygen source;
- European Patent 0 060 089 for a decomposltlon process wlth the nld of a reagent comprlslng a polyglycol and an alkallne hydrox~de ln the presence of oxygen.
Such processes have proven p~rtlally effectlve ln the sense that when they are carried out they present the maln risk of causlng the formntlon of hlghly toxlc products of decomposltlon and restructurlng of the molecule whlch lt ls wlshed to destroy, and everyone kno~s the dangers created by a decompositlon product of the dioxln type ln the case of the PCBs whlch ls obt~lned by degradation of the chlorinated molecules ln the presence of oxygen. We should also mentlon the very slgnlflcant formatlon of A volume of llberated gas of the types CO2 and N0~, a fact whlch necesslt~tes approprlate treatment equlpment.
Thus, the present lnventlon alms to prevent these dlsadvantnges and provldes a process for destroylng toxlc organlc molecules wlthout the rlsk of the dangers llsted Above, ln partlcular the formatlon of hlghly toxic degradatlon products, whlle at the same tlme reducln~ to a minlmum the volume of llberated gns, thls process belng characterlzed ln that lt comprlses as lts maln stage a vapo-cracklng operatlon.
Accordlng to an especlally advnntageous ~ethod to carry out this ~rQcessthls vapo-cracklng ls effected ln a reduclng medlu~ ln the presence of hydrogen.
128933~
l Accordlng to an ~dv~ntngeous method of conducting the prooess, the quantlty of hydrogen chosen ~s the reducing medlum ls between 1 nnd 1.5 Nm~/~g of the product to be tre~ted. The pr~sence of a reduclng medium of thls type results ln the preventlon of oxld~tlon of the organlc products le~dlng to hlghly toxlc dloxln-type by-products ln the case of the destructlon of ~ compound of the PCB famlly.
The tempernture of the reactlon ls adv~nt~geously 10 between 1000 nnd 1500-C.
Characterlstlcnlly, the process ls effected by an lnJectlon of superheated steam and oxyhydrogen combustlon.
Advant~geously, the quantlty of hydrogen needed for thls oxyhydrogen combustlon corresponds to an excess of 2 to 10 % ln relatlon to the stolchlometrlc condltlons.
Thus, in carrying out of thls process, the lnventlon covers all equlpment comprlslng R chamber for combustton and mlxlng wlth the admlsslon of hydrogen, oxygen and water vnpour; at least one reactor to recelve the mlxture resultlng from thls combustlon and the product to be treated and, at the exlt from thls reactor, statlons for the condensatlon and treatment of solld, llquld and gaseous reactlon products.
Other characterlstlcs nnd advantnges of the lnventlon wlll emerge more clearly from the followlng descrlptlon made wlth reference to the att~ched Flgure lllustratlng ln a hlghly diagrammntlc ~anner an equipment for carrying out the process of the lnventlon.
The equlpment shown ln the Flgure comprlses a known dlffuslon burner l, a combustlon Rnd mlxlng chamber 2, reactor 3, a condenser 4, ~ tank 5 for storlng the condensed products ~nd ~ pipe 17 ~or evncuatlng the gas to a conventlonal treatment devlce whlch 1~ not shown.
~2893:~4 l The diffuslon burner 1 comprlses a plpellne 6 for ln~ectlng hydrogen or nltrogen and a plpellne 7 for ln~ectlng oxygen or alr. These two plpellnes supply a plurallty of dlffusers. The dlffusion burner 1 also comprises ~ plpellne 8 for lnJectlng propane and oxygen supplylng the pllot llght and a clrcult 9 for supplylng w~ter to ensure coollng of the burner ~acket.
The combustlon ~nd mlxlng chamber 2, posltloned above the burner 1 ~nd comprislng a supply of w~ter vapour 10, ensures the adJustment of the temperature and the resldence tlme.
In the body of the reactor 3 there ls effected the lnJectlon of the product 11 to be treated, for example pyralene, ~nd of water vapour 12 servlng as a carrier ~nd purglng gas. The product 11 ls admltted ln an ultrasonlc resonance inJector requlrlng an adduct secondary fluld, for example water vapour 12. Thls allows pulverlsatlon to be lmproved and thereby the efflclency of the reactlon. The chamber 2 and the reactor 3 comprise ~pertures 13 and 13a for thermocouples and manometers for controlllng operatlon.
The condenser 4 comprises ln lts upper part a water feed plpe 15 ensurlng the condensatlon of the gas-coollng water and an lnlet 16 for ~ baslc product, for example dlluted sodlum hydroxide allowlng the neutralisatlon of the hydrogen chlorlde gAS formed ln the case of the treatment of chlorlnated products.
The operatlon of the apparatus comprlses the followlng st~ges:
- start-up:
. purglng of the plpellne 6 of hydrogen wlth an lnert gas such as nltrogen by dllutlon under pressure, . establlshment of coollng 9, .
1 . establlshment of flow of compressed ~lr lnto the dlffusers throu~h the plpellne 7, . start-up of the pilot llght, . establlshment of hydro~en flow - at the outset a S f1fth of the nomlnal flow, . replacement of the compressed alr by the oxygen ln the plpellne 7, . adJustment of the hydrogen and oxygen flows ln a stoichlometrlc manner durlng a flrst phase, . introductlon of the water vapour lnto the chamber 2, . extlnction of the pllot llght, . puttlng into thermal operatlon for one hour;
- reactlon:
. the destructlve reactlon occurs in the reactor 3, whlch ls preferably made of material reslstant at a temperature of 1500'C, for example refractory stalnless steel. The product, for example the pyralene, is lnJected lnto a plpellne 11 wlth the ald of a pump. The ultrasonlc resonance lnJector used requlres an auxlllary fluld, ln the present case w~ter vapour superheated to 120-C by a heatlng shaft. An aperture 13 for a thermocouple measures the ln~ection temperature ln the reactor, another aperture 13a allows the pressure to be me~sured. Flnally, an aperture 14 makes posslble the removal of the gases for analysls.
The hydrogen~oxygen reactlon ensures the calorlflc supply of the vapo-cr~cklng whlch, by dllution of the products by an lnert vapour, favours the decomposition of the molecules;
- recovery of the liquid, solid and gaseous dlscharges;
. an lnJectlon of water 15 completes the purlflc~tlon of the gases and the inJectlon of dlluted 33~''L
fi l sodlum hydroxide 16 ensures the neutrallzatlon of the hydrogen chlorlde gas resultlng from the reactlon of the hydro~en wlth the chlorlne llberated by the destructlon of the chlorlnated or~anic comDounds ;
. a tank 5 permlts the storage of the condensed llqulds whlle the ~ases are dlrected ~fter debubbllng to a conventlonal depollutlon system (not shown) whlch comprlses at lts outlet a propane~air excess gas burner for burning the excess hydrogen and the light hydrocarbons.
The followlng Example ls glven by way of lllustratlon and ln no way llmlts the present lnventlon.
Examp,Le Tr~al carried out wlth pyr~le~e 200 g of pyralene used ln transformers and containlng 60% polychlorblphenyl and 40%
trlchlorobenzene were lnJected lnto the reactor.
Chromatographlc me~surements have made lt posslble to show that 99.9985'~, of the pyralene was destroyed.
The by-products of decomposltlon comprlse notably naphthalene, blphenyl, phenanthrene, fluoranthene, and heavy hydrocarbons.
The llberated gases comprlse excess hydrogen and llght hydrocarbons: fractlon C2/C3; these gases are burned by the excess gas burner but may advantageously, ln large units, be used as a source of heat wlth a vlew to the productlon of water vapour necessary to the process.
~o tr~ce of dloxln was detected at the analysis threshold of the method, l.e. 2 ppm, <parts per mllllon~
for the by-products ~nd less than 15 ppt ~parts per trllllon) for the purlfylng waters.
The descriptlon of the present lnventlon has only been glven by way of lllustratlon ~nd ls in no way .
':
12139339~
,7 l llmltlng; ln fact lt is capable of belng varled ln dlverse ways wlthln lts scope and of allowlng treatment of all llquld, gaseous and solld organlc products, ln partlcular:
- pyralene cleanslng solvents, especlally freon, - products <lubrlcatlng olls and other solvents) contamlnated radloactlvely by metal salts partlcularly of the ceslum and cobalt types, for e~ample sclntlllatlon llqulds such as 1,5-dlphenyloxazole, 1,4-dl-2- (5-phenylo~azolyl) benzene etc. The metal lons formlng chelates, thls process decomposes these molecules, ensures thelr mlneralizatlon and the dlssolutlon of the radloactlve metal salts whlch, once ln aqueous phase, may then be easlly concentrated and treated by conventlonal processes of the nuclear lndustry.
The appllcatlons envlsaged thus relate to the treatment of waste from the electrlcal (transformers, condensers), chemlcal or lndeed nuclear lndustrles.
Moreover, lt wlll be clearly understood that the sources of hydrogen sultable for carrying out the process can be any. Thus especlally, thls hydrogen can be provlded by gas from coklng plants, flue gas or domestlc ~as, the quantltles of these gases used ln the process dependlng, of course, on thelr hydrogen content in order to fulfil the conditions of operation set forth in the pres`ent description concerning the quantity o~
hydrogen required.
l The present lnventlon relates to a process for destroylng organlc products wlth toxlc effects, preventlng pollutlon of the environment after an lncldent, accldent or any other case requlrlng these products to be deactlvated.
The inventlon also relates to the equlpment for carrying out thls process.
Xore preclsely, use ls currently belng made, ln certaln flelds of lndustry, of organlc compounds of, for example, the polychloroblphenyl type (usually called PCB> on account of thelr favourable characterlstlcs, especlally thelr good thermal stablllty, thelr good cbemlcal lnertness hnd thelr hlgh dlelectrlc constant 9 Justifylng thelr lntenslve use ln partlcular as flulds for transformers and/or condensers.
However, for some years studles have shown that such products are not blodegradable and that there ls evldence of thelr conslderable accumulatlon ln the food chaln. Furthermore, these studles h~ve shown that these products are hlghly toxlc and exhlbit behavlour whlch may be carclnogenlc~ In vlew of thls research, the governments of varlou~ countries concerned have lssued regulatlons rel~tlng to the use, stor~ge and destruction of these products. The result has been that varlous lndustrlal processes have been developed since then.
These processes generally lnvolve an o~eration of lnclneration wlth an excess of ~lr or oxygen ln devlces such ~s cement furn~ces or domestlc waste lnclner~tors.
Thus, one can clte:
'~ ~
' ~'' , :
~ . .
l - French Patent ~o. 2 323 432 for a c~talytlc decomposltion process of halo~enated organlc compounds;
- Pntent W0 82/0~509 for a decomposltlon process uslng a plasma burner operatlng at between 3000 and 4000 C;
- Patent W0 80~022116 for a decomposltion process uslng a fused salt and an oxygen source;
- European Patent 0 060 089 for a decomposltlon process wlth the nld of a reagent comprlslng a polyglycol and an alkallne hydrox~de ln the presence of oxygen.
Such processes have proven p~rtlally effectlve ln the sense that when they are carried out they present the maln risk of causlng the formntlon of hlghly toxlc products of decomposltlon and restructurlng of the molecule whlch lt ls wlshed to destroy, and everyone kno~s the dangers created by a decompositlon product of the dioxln type ln the case of the PCBs whlch ls obt~lned by degradation of the chlorinated molecules ln the presence of oxygen. We should also mentlon the very slgnlflcant formatlon of A volume of llberated gas of the types CO2 and N0~, a fact whlch necesslt~tes approprlate treatment equlpment.
Thus, the present lnventlon alms to prevent these dlsadvantnges and provldes a process for destroylng toxlc organlc molecules wlthout the rlsk of the dangers llsted Above, ln partlcular the formatlon of hlghly toxic degradatlon products, whlle at the same tlme reducln~ to a minlmum the volume of llberated gns, thls process belng characterlzed ln that lt comprlses as lts maln stage a vapo-cracklng operatlon.
Accordlng to an especlally advnntageous ~ethod to carry out this ~rQcessthls vapo-cracklng ls effected ln a reduclng medlu~ ln the presence of hydrogen.
128933~
l Accordlng to an ~dv~ntngeous method of conducting the prooess, the quantlty of hydrogen chosen ~s the reducing medlum ls between 1 nnd 1.5 Nm~/~g of the product to be tre~ted. The pr~sence of a reduclng medium of thls type results ln the preventlon of oxld~tlon of the organlc products le~dlng to hlghly toxlc dloxln-type by-products ln the case of the destructlon of ~ compound of the PCB famlly.
The tempernture of the reactlon ls adv~nt~geously 10 between 1000 nnd 1500-C.
Characterlstlcnlly, the process ls effected by an lnJectlon of superheated steam and oxyhydrogen combustlon.
Advant~geously, the quantlty of hydrogen needed for thls oxyhydrogen combustlon corresponds to an excess of 2 to 10 % ln relatlon to the stolchlometrlc condltlons.
Thus, in carrying out of thls process, the lnventlon covers all equlpment comprlslng R chamber for combustton and mlxlng wlth the admlsslon of hydrogen, oxygen and water vnpour; at least one reactor to recelve the mlxture resultlng from thls combustlon and the product to be treated and, at the exlt from thls reactor, statlons for the condensatlon and treatment of solld, llquld and gaseous reactlon products.
Other characterlstlcs nnd advantnges of the lnventlon wlll emerge more clearly from the followlng descrlptlon made wlth reference to the att~ched Flgure lllustratlng ln a hlghly diagrammntlc ~anner an equipment for carrying out the process of the lnventlon.
The equlpment shown ln the Flgure comprlses a known dlffuslon burner l, a combustlon Rnd mlxlng chamber 2, reactor 3, a condenser 4, ~ tank 5 for storlng the condensed products ~nd ~ pipe 17 ~or evncuatlng the gas to a conventlonal treatment devlce whlch 1~ not shown.
~2893:~4 l The diffuslon burner 1 comprlses a plpellne 6 for ln~ectlng hydrogen or nltrogen and a plpellne 7 for ln~ectlng oxygen or alr. These two plpellnes supply a plurallty of dlffusers. The dlffusion burner 1 also comprises ~ plpellne 8 for lnJectlng propane and oxygen supplylng the pllot llght and a clrcult 9 for supplylng w~ter to ensure coollng of the burner ~acket.
The combustlon ~nd mlxlng chamber 2, posltloned above the burner 1 ~nd comprislng a supply of w~ter vapour 10, ensures the adJustment of the temperature and the resldence tlme.
In the body of the reactor 3 there ls effected the lnJectlon of the product 11 to be treated, for example pyralene, ~nd of water vapour 12 servlng as a carrier ~nd purglng gas. The product 11 ls admltted ln an ultrasonlc resonance inJector requlrlng an adduct secondary fluld, for example water vapour 12. Thls allows pulverlsatlon to be lmproved and thereby the efflclency of the reactlon. The chamber 2 and the reactor 3 comprise ~pertures 13 and 13a for thermocouples and manometers for controlllng operatlon.
The condenser 4 comprises ln lts upper part a water feed plpe 15 ensurlng the condensatlon of the gas-coollng water and an lnlet 16 for ~ baslc product, for example dlluted sodlum hydroxide allowlng the neutralisatlon of the hydrogen chlorlde gAS formed ln the case of the treatment of chlorlnated products.
The operatlon of the apparatus comprlses the followlng st~ges:
- start-up:
. purglng of the plpellne 6 of hydrogen wlth an lnert gas such as nltrogen by dllutlon under pressure, . establlshment of coollng 9, .
1 . establlshment of flow of compressed ~lr lnto the dlffusers throu~h the plpellne 7, . start-up of the pilot llght, . establlshment of hydro~en flow - at the outset a S f1fth of the nomlnal flow, . replacement of the compressed alr by the oxygen ln the plpellne 7, . adJustment of the hydrogen and oxygen flows ln a stoichlometrlc manner durlng a flrst phase, . introductlon of the water vapour lnto the chamber 2, . extlnction of the pllot llght, . puttlng into thermal operatlon for one hour;
- reactlon:
. the destructlve reactlon occurs in the reactor 3, whlch ls preferably made of material reslstant at a temperature of 1500'C, for example refractory stalnless steel. The product, for example the pyralene, is lnJected lnto a plpellne 11 wlth the ald of a pump. The ultrasonlc resonance lnJector used requlres an auxlllary fluld, ln the present case w~ter vapour superheated to 120-C by a heatlng shaft. An aperture 13 for a thermocouple measures the ln~ection temperature ln the reactor, another aperture 13a allows the pressure to be me~sured. Flnally, an aperture 14 makes posslble the removal of the gases for analysls.
The hydrogen~oxygen reactlon ensures the calorlflc supply of the vapo-cr~cklng whlch, by dllution of the products by an lnert vapour, favours the decomposition of the molecules;
- recovery of the liquid, solid and gaseous dlscharges;
. an lnJectlon of water 15 completes the purlflc~tlon of the gases and the inJectlon of dlluted 33~''L
fi l sodlum hydroxide 16 ensures the neutrallzatlon of the hydrogen chlorlde gas resultlng from the reactlon of the hydro~en wlth the chlorlne llberated by the destructlon of the chlorlnated or~anic comDounds ;
. a tank 5 permlts the storage of the condensed llqulds whlle the ~ases are dlrected ~fter debubbllng to a conventlonal depollutlon system (not shown) whlch comprlses at lts outlet a propane~air excess gas burner for burning the excess hydrogen and the light hydrocarbons.
The followlng Example ls glven by way of lllustratlon and ln no way llmlts the present lnventlon.
Examp,Le Tr~al carried out wlth pyr~le~e 200 g of pyralene used ln transformers and containlng 60% polychlorblphenyl and 40%
trlchlorobenzene were lnJected lnto the reactor.
Chromatographlc me~surements have made lt posslble to show that 99.9985'~, of the pyralene was destroyed.
The by-products of decomposltlon comprlse notably naphthalene, blphenyl, phenanthrene, fluoranthene, and heavy hydrocarbons.
The llberated gases comprlse excess hydrogen and llght hydrocarbons: fractlon C2/C3; these gases are burned by the excess gas burner but may advantageously, ln large units, be used as a source of heat wlth a vlew to the productlon of water vapour necessary to the process.
~o tr~ce of dloxln was detected at the analysis threshold of the method, l.e. 2 ppm, <parts per mllllon~
for the by-products ~nd less than 15 ppt ~parts per trllllon) for the purlfylng waters.
The descriptlon of the present lnventlon has only been glven by way of lllustratlon ~nd ls in no way .
':
12139339~
,7 l llmltlng; ln fact lt is capable of belng varled ln dlverse ways wlthln lts scope and of allowlng treatment of all llquld, gaseous and solld organlc products, ln partlcular:
- pyralene cleanslng solvents, especlally freon, - products <lubrlcatlng olls and other solvents) contamlnated radloactlvely by metal salts partlcularly of the ceslum and cobalt types, for e~ample sclntlllatlon llqulds such as 1,5-dlphenyloxazole, 1,4-dl-2- (5-phenylo~azolyl) benzene etc. The metal lons formlng chelates, thls process decomposes these molecules, ensures thelr mlneralizatlon and the dlssolutlon of the radloactlve metal salts whlch, once ln aqueous phase, may then be easlly concentrated and treated by conventlonal processes of the nuclear lndustry.
The appllcatlons envlsaged thus relate to the treatment of waste from the electrlcal (transformers, condensers), chemlcal or lndeed nuclear lndustrles.
Moreover, lt wlll be clearly understood that the sources of hydrogen sultable for carrying out the process can be any. Thus especlally, thls hydrogen can be provlded by gas from coklng plants, flue gas or domestlc ~as, the quantltles of these gases used ln the process dependlng, of course, on thelr hydrogen content in order to fulfil the conditions of operation set forth in the pres`ent description concerning the quantity o~
hydrogen required.
Claims (10)
1. A process for destroying organic products with toxic effects, such as waste from the electrical, chemical or nuclear industries, without the risk of forming secondary decomposition products which are equally toxic, comprising as its main stage a vapo-cracking operation.
2. A process according to claim 1, wherein the said vapo-cracking is effected in a reducing medium in the presence of hydrogen.
3. A process according to claim 2, wherein the quantity of hydrogen is between 1 and 1.5 Nm3/kg of the product to be treated.
4. A process according to claim 2 wherein the hydrogen needed is supplied by an industrial gas or by domestic gas.
5. A process according to claim 3 wherein the hydrogen needed is supplied by an industrial gas or by domestic gas.
6. A process according to claim 4 or claim 5 wherein the industrial gas is a coking plant gas or a flue gas.
7. A process according to claim 1, wherein the vapo-cracking reaction is effected at a temperature of between 1000 and 1500° C.
8. A process according to claim 1, wherein the vapo cracking is effected by or with the superheated water vapour and oxyhydrogen combustion.
9. A process according to claim 8, wherein the quantity of hydrogen necessary for oxyhydrogen combustion corresponds to an excess of 2 to 10% in relation to the stoichiometric conditions.
10. Equipment for carrying out the process according to claim 1, comprising a combustion and mixing chamber with admission of hydrogen, oxygen and water vapour; at least one reactor to receive the mixture from the combustion chamber and the product to be treated and, at the exit from this reactor, stations for condensing and treating the products of the reaction.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR8516.133 | 1985-10-30 | ||
| FR8516133A FR2589372B1 (en) | 1985-10-30 | 1985-10-30 | PROCESS FOR DESTRUCTION OF ORGANIC PRODUCTS WITH TOXIC EFFECTS AND PLANT FOR CARRYING OUT SAID METHOD |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1289334C true CA1289334C (en) | 1991-09-24 |
Family
ID=9324361
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000521262A Expired - Lifetime CA1289334C (en) | 1985-10-30 | 1986-10-23 | Process for destroying organic products with toxic effects and equipment for implementing this process |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0235473B1 (en) |
| JP (1) | JPS62127069A (en) |
| AT (1) | ATE47322T1 (en) |
| AU (1) | AU588390B2 (en) |
| CA (1) | CA1289334C (en) |
| DE (1) | DE3666354D1 (en) |
| ES (1) | ES2011454B3 (en) |
| FR (1) | FR2589372B1 (en) |
| GR (1) | GR3000228T3 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113108291A (en) * | 2021-04-22 | 2021-07-13 | 红河州现代德远环境保护有限公司 | Device for pretreating dichloroethane by pyrogenic process |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3942962A1 (en) * | 1989-12-23 | 1991-06-27 | Kammerer F Gmbh | METHOD FOR DISPOSAL OF SUBSTANCES CONTAINING HALOGENED HYDROCARBON COMPOUNDS OR MIXTURES THEREOF, AND DEVICE FOR CARRYING OUT THE METHOD |
| FR2686347B1 (en) * | 1992-01-22 | 1994-10-07 | Lorraine Carbone | METHOD OF PYROLYSIS OF FLUID EFFLUENTS AND CORRESPONDING DEVICE. |
| DE19948203A1 (en) * | 1999-10-06 | 2001-04-12 | Solvay Fluor & Derivate | Thermal decomposition of halogenated carbon compounds |
| JP4695293B2 (en) * | 2001-05-30 | 2011-06-08 | 株式会社眞誠 | Condensate discharge device for rapid cooling device |
| WO2013084324A1 (en) | 2011-12-07 | 2013-06-13 | トヨタ自動車株式会社 | Vehicle body lower structure |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5530867B2 (en) * | 1973-01-16 | 1980-08-14 | ||
| NO762638L (en) * | 1975-09-15 | 1977-03-22 | Continental Oil Co | PROCEDURES FOR DECOMPOSITION OF HALOGENATED ORGANIC COMPOUNDS. |
| US4351978A (en) * | 1980-07-21 | 1982-09-28 | Osaka Prefectural Government | Method for the disposal of polychlorinated biphenyls |
| WO1982002001A1 (en) * | 1980-12-08 | 1982-06-24 | Vasak Vladimir | Waste disposal |
-
1985
- 1985-10-30 FR FR8516133A patent/FR2589372B1/en not_active Expired
-
1986
- 1986-10-23 CA CA000521262A patent/CA1289334C/en not_active Expired - Lifetime
- 1986-10-29 EP EP86402425A patent/EP0235473B1/en not_active Expired
- 1986-10-29 AT AT86402425T patent/ATE47322T1/en not_active IP Right Cessation
- 1986-10-29 JP JP61258089A patent/JPS62127069A/en active Pending
- 1986-10-29 AU AU64491/86A patent/AU588390B2/en not_active Ceased
- 1986-10-29 DE DE8686402425T patent/DE3666354D1/en not_active Expired
- 1986-10-29 ES ES86402425T patent/ES2011454B3/en not_active Expired - Lifetime
-
1989
- 1989-11-29 GR GR89400260T patent/GR3000228T3/en unknown
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113108291A (en) * | 2021-04-22 | 2021-07-13 | 红河州现代德远环境保护有限公司 | Device for pretreating dichloroethane by pyrogenic process |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62127069A (en) | 1987-06-09 |
| EP0235473B1 (en) | 1989-10-18 |
| GR3000228T3 (en) | 1991-03-15 |
| ES2011454B3 (en) | 1990-01-16 |
| ATE47322T1 (en) | 1989-11-15 |
| FR2589372A1 (en) | 1987-05-07 |
| AU6449186A (en) | 1987-05-07 |
| FR2589372B1 (en) | 1988-02-05 |
| EP0235473A1 (en) | 1987-09-09 |
| DE3666354D1 (en) | 1989-11-23 |
| AU588390B2 (en) | 1989-09-14 |
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