EP0354731A1 - Procédé et dispositif pour la pyrolyse à plasma de déchets liquides - Google Patents

Procédé et dispositif pour la pyrolyse à plasma de déchets liquides Download PDF

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Publication number
EP0354731A1
EP0354731A1 EP89307930A EP89307930A EP0354731A1 EP 0354731 A1 EP0354731 A1 EP 0354731A1 EP 89307930 A EP89307930 A EP 89307930A EP 89307930 A EP89307930 A EP 89307930A EP 0354731 A1 EP0354731 A1 EP 0354731A1
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EP
European Patent Office
Prior art keywords
gases
waste material
water
chamber
scrubber
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP89307930A
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German (de)
English (en)
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EP0354731B1 (fr
Inventor
Robert Chrong-Wen Chang
Michael Fraser Joseph
Steven Christian Vorndran
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CBS Corp
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Westinghouse Electric Corp
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Publication date
Application filed by Westinghouse Electric Corp filed Critical Westinghouse Electric Corp
Publication of EP0354731A1 publication Critical patent/EP0354731A1/fr
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Publication of EP0354731B1 publication Critical patent/EP0354731B1/fr
Expired legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B19/00—Heating of coke ovens by electrical means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form

Definitions

  • This invention relates to an apparatus and to a method for pyrolytically decomposing waste material, and in particular, it pertains to apparatus and method for disposing of toxic and hazardous materials by pyroplasmic decomposition.
  • waste material is a growing problem due primarily to the fact that the volume of waste material is growing faster than existing disposal equipment and methods can handle it economically.
  • Most attempts to dispose of waste materials by combustion have included furnaces or rotary kilns.
  • apparatus and methods for waste destruction have included plasma pyrolysis, such as disclosed in the specification of U.S. Patent No. 4,644,877, by which waste materials are fed into a plasma arc burner where they are atomized, ionized, and subsequently discharged into a reaction chamber to be cooled and recombined into product gases and particulate matter.
  • the method of this patent involves the use of a solvent that is miscible with the waste materials, such as methyl ethyl ketone with PCBS.
  • a method for pyrolytically decomposing waste material includes the steps of producing a plasma by use of oxygen as the torch gas, atomizing waste material and a source of hydrogen and oxygen, then injecting the atomized waste material and source of hydrogen and water into the plasma, having a temperature in excess of 5000°C to form a mixture of produce gases and solid particulate, separating the gases and particulate mixture in a recombination chamber into separate phases of gases and solid particulate, transferring the solid particulate to separate compartment and subjecting the particulate to a partial vacuum to separate any carryover gases from the particulate which carryover gases are combined with the gases from the recombination chamber, transferring the gas from the recombination chamber to a scrubber and subjecting the gas to a water spray to eliminate any carryover solid particulate from the gases, and removing the scrubbed gases from the scrubber.
  • the invention includes an apparatus for pyrolytically decomposing waste material
  • a plasma torch productive of a plasma having an operating temperature of at least 5000°C to destroy a solution of a waste material to form a mixture of gases and solid particulate, said torch in co-operation with means for introducing the waste material in an atomized state, a recombination chamber adatped to receive and separate the mixture of gases and solid particulate, a separator to provide a partial vacuum to remove any carryover gases from the solid particulate, a transfer chamber to receive gases from the recombination chamber, a scrubber to clean the gases from the chamber by passing the gases through a water spray, and storage means for gases from the scrubber.
  • the invention involves a method for the pyrolytic destruction of waste material including the steps of mixing the waste material, water, and/or methanol into a plasma arc having a temperature in excess of 5000°C to form a mixture of product gases and solid particulate, separating the gases and the particulate mixture in a recombination chamber into separate phases of gases and solid particulate; transferring the solid particulate to a separate compartment and subjecting the particulate to a partial vacuum to separate any carry-over gases from the particulate which carry-over gases are conbined with the gases from the recombination chamber; transferring the gas from the recombination chamber to a scrubber and subjecting the gas to a water spray to eliminate any carry-over solid particulate from the gases; and removing the scrubbed gases from the product gas stream.
  • the apparatus for pyrolytically decomposing waste material comprises a plasma torch productive of an electric arc having an operating temperature of at least 5000°C for incinerating a solution of waste material to form a mixture of gases and solid particulate; a recombination chamber for receiving and separating the mixture of gases and solid particulate; a solid separator for providing a partial vacuum for removing any carry-over gases from the solid particulate; a transfer chamber for receiving gases from the recombina­tion chamber; a scrubber for cleaning the gas from the transfer chamber by passing the gas through a water spray; and storage means for gases from the scrubber.
  • the transfer chamber is a combustion chamber for the gases and the burned gases are directed to a draft means, such as a stack, for delivery of the burned gases into the atmosphere.
  • An advantage of this method and apparatus is that there is at least a threefold increase in the feed throughput with a reduction of the flue gas volume compared with prior art procedures.
  • This process removes the free carbon directly from the recombination chamber and flares the product gases in the combustion chamber.
  • the high heating values of the product gases can bypass the combustion process for other use by closing the combustion air stream.
  • a system for pyrolytically decomposing waste material of an existing, or prior art, method is shown diagrammatically in Figure 1. It comprises a plasma torch 5, a recombination chamber 7, a scrubber 9, a draft fan 11, an inertial trap 13, and a stack 15.
  • the plasma torch by which the process of this invention is preferably performed includes a so-called arc heater which is similar in construction and operation to that disclosed in the specifications of U.S. Patent Nos. 3,765,870; 3,791,949; and 4,644,877 in which an electric arc extends between spaced electrodes with the generation of heat for the destruction of hazardous and toxic wastes.
  • Waste material is fed into the torch 15 at inlet 17 together with a solvent at an inlet 19.
  • a typical waste material is hazardous and toxic and contains a mixture of about 60% polychlorinated biphenyls (PCB) and of about 40% trichlorobenzene (TCB) which is derived from the operation of electric transformers and is commonly referred to as Askarel.
  • Liquid waste material is introduced into the torch feed inlet 17 which together with a solvent comprising a mixture of methyl ethyl ketone (MEK) (50% by weight) and methanol (50%) is introduced (Fig. 1) to supply the hydrogen source to produce hydrogen chloride (HCl).
  • MEK methyl ethyl ketone
  • the mixture of the feed and solvent is processed at the high temperatures of operation of the plasma arc, typically ranging from 5000°C to 15,000°C, forming a mixture of product gases and solid particulate, which is directed into the recombination chamber 7, where in the presence of air introduced at inlet 21, produces a gaseous mixture consisting of H2O, H2, CO, CO2, N2, and HCl.
  • the gaseous mixture is then directed into the scrubber 9 where a caustic solution of water (NaOH + H2O) sprays at 22 the gaseous mixture to eliminate solid particulates and to convert the HCl to NaCl mixed with water.
  • the resulting blow-down water containing NaCl and carbon particulate is drained from the scrubber at outlet 23.
  • the draft fan 11 transfers the gas from the scrubber 9 to the inertial trap 13 where it is subjected to additional water spray 25 to further eliminate carbon particulate. Blow-down water is drained at 26. From the inertial trap 13 the gas products are flared and vented into the atmosphere through the stack 27.
  • the torch 15 (Fig. 2) provides a high tempera­ture ionized, conductive gas that is created within the torch.
  • the torch comprises a pair of cylindrical electrodes 28, 29 that are longitudinally spaced by a gap 31, into which a pressurized gas, such as air, is injected to blow an electric arc 33 into the interior of the torch.
  • a pressurized gas such as air
  • the upstream and downstream ends of the arc are located on the electrodes 28, 29.
  • An annular nozzle 35 is located between the electrode 29 and a burner chamber 37 that is contained within a cylindrical insulation 39 through which the plasma plume 41 extends.
  • the nozzle 35 includes a plurality of peripherally spaced, radially extending inlets 43.
  • the prior art procedure involves the use of a mixture of a solvent of MEK and methanol with the waste material (Askarel) which mixture is introduced into the torch 15 through the inlets 43 of the nozzle 35.
  • This prior art procedure processes about 0.1 gallons of PCB per minute. It is noted that the solvent mixture of MEK and methanol is miscible with the PCB and air is used as torch gas to create plasma.
  • the solution is water, which is immiscible with non-polar type waste material, such as PCB and TCB.
  • the water which is mixed with the waste material before introduction into the plasma torch. Pure oxygen (not air) is used as the torch gas. Water supplies hydrogen and oxygen that allows for an increased throughput of waste at a rate of up to twelve times that which is possible in the prior art system of Fig 1.
  • the waste material or feed is the Askarel fluid.
  • An alternate method to preliminarily mixing the feed and water is to inject the feed and water separately through an air atomizing nozzle into the torch.
  • the amount of water mixed with waste is from about 30% to 200% by wt.
  • the preferred amount of water is about 50% that of waste.
  • the system for pyrolytically decomposing waste material of this invention preferably involves the use of the flow diagram of Figure 3.
  • the apparatus includes a plasma torch 43, a recombination chamber 45, a combustion chamber 47, a scrubber 49, a draft fan 51, a stack 53, and a storage tank 55.
  • the torch 43 ( Figure 4) provides a high temperature ionized, conductive gas which is created within the torch by the interaction of a gas with an electric or plasma arc 57 produced by the torch 43.
  • the interaction within the torch 43 disassociates the gas into electrons and ions which cause the gas to become both thermally and electrically conductive.
  • the conductive properties of the ionized gas in the arc region provides a means to transfer energy from the arc to the incoming process gas. This state is called a "plasma" and exists within the immediate confines of the arc in the torch and is superheated to an extremely high temperature having a typical range of from 5000°C to 15,000°C.
  • the extremely high temperatures and the ultraviolet radiation associated with the ionized superheated gases provides sufficient bond breaking energy to destroy the hazardous and toxic wastes.
  • This pyrolytic process is designed to destroy pumpable liquid/solid mixtures with the pyroplasma arc torch 43.
  • the feed is injected through a plurality of air atomizing nozzles 59 (Fig. 4) into a manifold 61 where it is mixed with air before it encounters with the plasma plume 57 at temperatures in excess of 5000°C.
  • the com­pounds in the feed are reformed into compounds which are more stable at reactor temperatures according to basic thermodynamic equilibrium principles.
  • the water (without methanol) and feed are mixed homogeneously and introduced through a feed inlet 63 and air enters through an air inlet 65.
  • the air atomizing nozzle 59 receives the waste feed that is mixed with water and/or methanol (up to 25%) and conducted through a static mixer 67, after which it is combined with compressed air at 69.
  • the waste feed 63 is introduced into the manifold 61 which is secured to the recombination chamber 45 by a mounting flange 71.
  • the manifold 61 is annular and is disposed between an outer housing 72 and a sleeve 73 which is comprised of refractory or silicon carbide coated graphite.
  • the waste feed 63 is mixed with the air 65 and is emitted through outlets 75 to form a flame zone 77 with the plasma 79 which zone is the result of partial combustion of waste feed mixtures.
  • the plasma 79 results from the combination of the electric arc 57 and torch gas 81 introduced through a gap 83 between cylindrical electrodes 85, 87 of the plasma torch 43. The resulting products are projected into the recombination chamber 45.
  • the plasma system of this invention usually operates in a slightly reducing atmosphere and the resulting flue gases are mostly H2, CO, CO2, C, N2, H2O, and HCl. From a thermodynamic standpoint all of the chlorine forms HCl because of the high concentrations of H2 and low concentrations of 02. Therefore, there are no free or very low Cl2, O2, Cl, and OH radicals to form dioxins and furans.
  • the product gases together with solid particulate, such as carbon enter the recombination chamber 45 which is an air filter such as a cyclone separator.
  • the product gases and solid particu­late entering the recombination chamber 45 have tempera­tures ranging from 1000° to 1500°C with a preferred temperature of 1200°C.
  • the product gases exit through an outlet 89 and through a valve 91 to the combustion chamber 47.
  • the dominant portion of the solid particulate 93 settles at the bottom of the chamber 45. There it accumulates until it is dumped.
  • a high temperature dump valve 95 is provided in the bottom wall of the chamber 45 which valve comprises an elongated tube 97 in which a sliding stopper rod 99 is slidably mounted.
  • a rod actuator 101 is provided for lowering the rod in order to open the tube 97 to enable the accumulated solid particulate 93 to drop through the tube and through a conduit 103 into a separator 105.
  • the purpose of the separator is to remove any carry-over gases which are mixed with the particulate in the recombination chamber 45.
  • the separator 105 is a cyclone separator into which the solid particulate enters from the conduit 103 with sufficient centrifugal force to throw the solid particulate out against the wall and drop into the lower portion of the separator tank.
  • the separated gas exits from the separator 105 through a filter 107 and through a conduit 109 and a valve 111 from where it is conducted to the combustion chamber 47.
  • a heat exchanger having a coolant inlet 113 and a coolant outlet 115 is provided to cool the accumulated gas-free solid particulate 93 .
  • the solid particulate 93 is discharged from the separator 105 through a discharge valve.
  • the purpose of the filter 107 is to filter out any remaining solid particulate that may be carried by the gas as it exits from the separator 105.
  • the gases exit from the chamber through a filter 119 and into the outlet 89.
  • the filter 119 like the filter 107 eliminates most of the particulate that may be carried by the gas into the outlet 89 and therefrom into the combustion chamber 47.
  • the valve 91 is open and the valve 111 in the conduit 109 is closed. Inasmuch as the entire system is closed, the draft fan 51 sustains a partial vacuum through the several parts 45, 47, 49, and the interconnecting conduits therebetween. Accordingly, the gas moves from the recombination chamber 45 through the conduit 119 when valve 91 is opened.
  • valve 91 is closed and valve 111 is opened, whereby the gas leaving the separator 105 is carried through the conduit 109 to the combustion chamber 47 in response to the partial vacuum created by the draft fan 51.
  • the combustion chamber 47 has a primary function of burning the process gases (H2, CO, CO2, N2, H2O, HCl) which enter the chamber.
  • process gases H2, CO, CO2, N2, H2O, HCl
  • an air inlet 123 is provided to convert those gases to a gas mixture comprising CO2, H2O, N2, and HCl. Thereafter the gas mixture moves through the scrubber 49.
  • a secondary function of the combustion chamber 47 is to act as a conduit for the product gases leaving the recombination chamber 45.
  • the gas leaves the combustion chamber 47 through a conduit 125 into the scrubber where it is subjected to a water spray having an inlet 127 in order to eliminate any solid particulate which lingers in the gas.
  • the resulting blow-down water 129 containing particulate accumulates in the lower portion of the scrubber 49 from where it is periodically drained through an outlet 131.
  • a caustic solution is introduced into the water at 133 for the purpose of converting the HCl in the gas to a chloride compound.
  • a preferred caustic solution is sodium hydroxide (NaOH) which reacts with the HCl in accordance with the following formula: NaOH + HCl NaCl + H2O.
  • NaOH sodium hydroxide
  • the resulting compound (NaCl) is drained from the scrubber with the blow-down water 129.
  • the resulting gas mixture includes CO2, H2O, and N2 which move through a conduit 135 through the draft fan and through a conduit 137 to the stack 53 where it is dissipated into the atmosphere as a non-toxic gas and devoid of solid particulate.
  • the combustion chamber 47 serves as a mere conduit for the product gases entering through the conduit 109, without being burned, the gases pass through the scrubber 49. Again the gases are subjected to the caustic solution to eliminate the HCl and exit from the scrubber via the conduit 135 as combustable fuel consisting of H2, CO, CO2, N2, and H2O. From the draft fan 51 the fuel is diverted by a valve 139 and through a conduit 141 to the storage tank 55 from which the fuel is withdrawn as required.
  • the foregoing system includes a recycle means for reintroducing the water into the scrubber at 127.
  • some of the blow-­down water is eliminated at outlet 143 with the remaining blow-down water moving through a liquid solid separator 143 and a heat exchanger 145.
  • the liquid solid separator 143 functions to eliminate any lingering solid part­iculate.
  • the heat exchanger 145 functions to adjust the water to the desired temperature. Manifestly, any caustic solution remaining in the blow-down water in the scrubber tank is recirculated to the scrubber tank for the purpose intended.
  • the system of this invention increases the feed throughput at least three gallons/minute and dramatically reduces the fuel gas volume over the system shown in Figure 1.
  • the system of this invention also removes the free carbon directly from the recombination chamber and flares the product gas in the combustion chamber.
  • the high heating values of the product gases can bypass the combustion process for other usage by closing the combustion air inlet 123.
  • the principle of the solid removal system is initially based on high temperature dump valve 95 which is opened at designated intervals. When the dump valve is closed, valve 91 is opened while valve 111 is closed. Conversely, when the dump valve 95 is opened, valve 91 is closed and valve 111 is opened.
  • the feed system of prior art injects the waste feed solution directly into the plasma arc to produce a lot of undesirable carbon especially when processing the chlorinated aromatic compounds.
  • the feed system of the system of Fig. 4 alleviates the carbon formation by mixing air or oxygen before it contacts with the plasma plume.
  • the recombination chamber 45 of this method removes most of the solid before entering the combustion chamber. Because the recombination chamber separates most of the particulate, a higher feed through­out the plasma torch is possible compared to the prior art. At the same time larger particles of particulate can be fed because it is readily eliminated through the solid separator.
  • combustion chamber may be used as a conduit for the product gases from the recombustion chamber without burning the gases so that the gases may be used as a fuel instead of being flared and discarded through the stack.
  • water consumption can be reduced by recycling the blowdown water from the scrubber.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treating Waste Gases (AREA)
EP19890307930 1988-08-10 1989-08-03 Procédé et dispositif pour la pyrolyse à plasma de déchets liquides Expired EP0354731B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US22988488A 1988-08-10 1988-08-10
US229884 1988-08-10

Publications (2)

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EP0354731A1 true EP0354731A1 (fr) 1990-02-14
EP0354731B1 EP0354731B1 (fr) 1992-05-20

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EP (1) EP0354731B1 (fr)
JP (1) JP2756505B2 (fr)
CA (1) CA1324823C (fr)
DE (1) DE68901592D1 (fr)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1991013532A1 (fr) * 1990-02-26 1991-09-05 Maschinen- Und Anlagenbau Grimma Gmbh Plasmatron a vapeur d'eau comme gaz de plasma et procede de fonctionnement stable du plasmatron
US5206879A (en) * 1990-08-03 1993-04-27 Tioxide Group Services Limited Destruction process
WO1993017759A1 (fr) * 1992-03-04 1993-09-16 Commonwealth Scientific And Industrial Research Organisation Traitement de materiaux
DE4231771A1 (de) * 1992-09-23 1994-03-24 Bayer Ag Verfahren zur Verstromung von Kunststoffabfällen
AU669158B2 (en) * 1992-03-04 1996-05-30 Srl Plasma Pty Ltd Material processing
WO1996041505A1 (fr) * 1995-06-07 1996-12-19 Physical Sciences, Inc. Appareil a hyperfrequence, de pulverisation a plasma, et procede de pulverisation
WO1997022556A1 (fr) * 1995-12-20 1997-06-26 Alcan International Limited Reacteur thermique a plasma et procede de traitement d'eau de decharge
GB2490175A (en) * 2011-04-21 2012-10-24 Tetronics Ltd Treatment of waste
CN109737430A (zh) * 2019-01-03 2019-05-10 鲁西化工集团股份有限公司硅化工分公司 一种危险废物处理***及方法

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH089168B1 (fr) * 1992-09-07 1996-01-31
FR2866414B1 (fr) * 2004-02-18 2006-03-17 Commissariat Energie Atomique Dispositif et procede de destruction de dechets liquides, pulverulents ou gazeux par plasma inductif
JP4827520B2 (ja) 2005-12-21 2011-11-30 出光興産株式会社 樹脂ペレット貯蔵装置及びその清掃方法
JP2007296415A (ja) * 2006-03-14 2007-11-15 Nippon Steel Corp ポリ塩化ビフェニル汚染物の処理方法及びその処理システム

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3828162A (en) * 1964-10-01 1974-08-06 Ppg Industries Inc Method for heating corrosive gases with arc heater
WO1982000509A1 (fr) * 1980-07-25 1982-02-18 I Faeldt Procede et appareil de decomposition thermique de composes stables
GB2113815A (en) * 1982-01-18 1983-08-10 Skf Steel Eng Ab Method and plant for conversion of waste material to stable final products
US4644877A (en) * 1984-01-23 1987-02-24 Pyroplasma International N.V. Plasma pyrolysis waste destruction

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3828162A (en) * 1964-10-01 1974-08-06 Ppg Industries Inc Method for heating corrosive gases with arc heater
WO1982000509A1 (fr) * 1980-07-25 1982-02-18 I Faeldt Procede et appareil de decomposition thermique de composes stables
GB2113815A (en) * 1982-01-18 1983-08-10 Skf Steel Eng Ab Method and plant for conversion of waste material to stable final products
US4644877A (en) * 1984-01-23 1987-02-24 Pyroplasma International N.V. Plasma pyrolysis waste destruction

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1991013532A1 (fr) * 1990-02-26 1991-09-05 Maschinen- Und Anlagenbau Grimma Gmbh Plasmatron a vapeur d'eau comme gaz de plasma et procede de fonctionnement stable du plasmatron
US5498826A (en) * 1990-02-26 1996-03-12 Maschinen- Und Anlagenbau Grimma Gmbh (Mag) Plasmatron with steam as the plasma gas and process for stable operation of the plasmatron
US5206879A (en) * 1990-08-03 1993-04-27 Tioxide Group Services Limited Destruction process
WO1993017759A1 (fr) * 1992-03-04 1993-09-16 Commonwealth Scientific And Industrial Research Organisation Traitement de materiaux
AU669158B2 (en) * 1992-03-04 1996-05-30 Srl Plasma Pty Ltd Material processing
DE4231771A1 (de) * 1992-09-23 1994-03-24 Bayer Ag Verfahren zur Verstromung von Kunststoffabfällen
WO1996041505A1 (fr) * 1995-06-07 1996-12-19 Physical Sciences, Inc. Appareil a hyperfrequence, de pulverisation a plasma, et procede de pulverisation
US5793013A (en) * 1995-06-07 1998-08-11 Physical Sciences, Inc. Microwave-driven plasma spraying apparatus and method for spraying
US5973289A (en) * 1995-06-07 1999-10-26 Physical Sciences, Inc. Microwave-driven plasma spraying apparatus and method for spraying
WO1997022556A1 (fr) * 1995-12-20 1997-06-26 Alcan International Limited Reacteur thermique a plasma et procede de traitement d'eau de decharge
US6187206B1 (en) 1995-12-20 2001-02-13 Alcan International Thermal plasma reactor and wastewater treatment method
GB2490175A (en) * 2011-04-21 2012-10-24 Tetronics Ltd Treatment of waste
US9744575B2 (en) 2011-04-21 2017-08-29 Tectronics (International) Limited Treatment of waste
CN109737430A (zh) * 2019-01-03 2019-05-10 鲁西化工集团股份有限公司硅化工分公司 一种危险废物处理***及方法

Also Published As

Publication number Publication date
CA1324823C (fr) 1993-11-30
JP2756505B2 (ja) 1998-05-25
EP0354731B1 (fr) 1992-05-20
JPH0283079A (ja) 1990-03-23
DE68901592D1 (de) 1992-06-25

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