WO1994023802A1 - Procede et appareil destines a detruire des dechets organiques et contenant des hydrocarbures - Google Patents

Procede et appareil destines a detruire des dechets organiques et contenant des hydrocarbures Download PDF

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Publication number
WO1994023802A1
WO1994023802A1 PCT/US1994/003912 US9403912W WO9423802A1 WO 1994023802 A1 WO1994023802 A1 WO 1994023802A1 US 9403912 W US9403912 W US 9403912W WO 9423802 A1 WO9423802 A1 WO 9423802A1
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WO
WIPO (PCT)
Prior art keywords
reaction
molten salt
gaseous
products
waste
Prior art date
Application number
PCT/US1994/003912
Other languages
English (en)
Inventor
S. Garry Howell
Lloyd M. Watson
Richard H. Scott
Martin Krynen
Original Assignee
Wabash, Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Wabash, Inc. filed Critical Wabash, Inc.
Priority to NZ265199A priority Critical patent/NZ265199A/en
Priority to AU65572/94A priority patent/AU696437B2/en
Publication of WO1994023802A1 publication Critical patent/WO1994023802A1/fr

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Classifications

    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D3/00—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances
    • A62D3/30—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents
    • A62D3/32—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents by treatment in molten chemical reagent, e.g. salts or metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/0075—Disposal of medical waste
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C1/00—Reclamation of contaminated soil
    • B09C1/06—Reclamation of contaminated soil thermally
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C1/00—Reclamation of contaminated soil
    • B09C1/08—Reclamation of contaminated soil chemically
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D2101/00—Harmful chemical substances made harmless, or less harmful, by effecting chemical change
    • A62D2101/40—Inorganic 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
    • A62D2101/40—Inorganic substances
    • A62D2101/43—Inorganic substances containing heavy metals, in the bonded or free state
    • 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
    • A62D2101/40—Inorganic substances
    • A62D2101/45—Inorganic substances containing nitrogen or phosphorus
    • 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
    • A62D2101/40—Inorganic substances
    • A62D2101/49—Inorganic 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

Definitions

  • This invention relates to a process and apparatus for destroying the organic or carbonaceous portion of various wastes, including polyhalogenated polyphenyls, paint sludge, chrome tannery waste, aluminum pot liners, contaminated soil, hospital waste, hydrocarbon-containing sludges, and mixtures thereof.
  • a molten salt solution comprising an alkali metal nitrate and an alkali metal carbonate
  • reacting the organic portion of the waste material with said molten salt solution in order to form gaseous carbon dioxide, water vapor and gaseous and non-gaseous reaction by-products, and to reduce at least a portion of said nitrate into the corresponding nitrite, thereby destroying said waste; and venting said gaseous carbon dioxide, said water vapor and said gaseous by-products.
  • the nitrate be sodium nitrate and the carbonate be sodium carbonate.
  • an additional step of regenerating said alkali metal nitrate by converting said alkali metal nitrite into said nitrate be employed, wherein said regeneration is performed by contacting at least a portion of said molten solution containing said nitrite with a gaseous stream containing oxygen.
  • the reaction of the waste and the molten salt may occur directly in the reservoir itself, or in a reaction unit.
  • the reaction unit can be a packed column, a spray scrubber, a venturi scrubber, or similar gas-liquid contacting device. If the reaction takes place in the reservoir, a packed column is placed in fluid communication with the reservoir, and gaseous reaction by-products will enter the column.
  • Molten salt is then contacted with these by-products within this column to further destroy any organic materials remaining.
  • waste materials which can be destroyed by this process include paint sludge, chrome tannery waste, contaminated soil, hospital waste, polyhalogenated polyphenyl-containing waste, hydrocarbon-containing sludge, and mixtures thereof.
  • An alternative embodiment utilizes an angled reaction pipe, having a screw rotatably attached to said reaction pipe for moving any solid waste or by-products present along the length of said reaction pipe, and further comprising a means for feeding said molten salt into said reaction pipe.
  • a perforated drum may also be employed as a reaction unit for destroying the organic portion of a waste.
  • the waste material to be destroyed is mixed with an alkali material and an alkali metal nitrate to form a reaction mixture; this mixture is then heated in a reaction unit in order to initiate a reaction between said organic portion, said nitrate and said alkali material, said reaction causing said organic portion to be destroyed.
  • This reaction is permitted to continue until substantially all of said organic portion is converted into gaseous carbon dioxide, water vapor, and gaseous and non- gaseous by-products; said carbon dioxide, said water vapor and said gaseous by-products are then vented from said reaction unit, and said non- gaseous by-products and said inorganic portion of said waste material are removed from said reaction unit.
  • the reaction unit for this latter embodiment may be a heated reaction trough having a rotating screw therein, said trough being heated by molten salt flowing through a salt jacket.
  • Figure 1 is a schematic of one embodiment of an apparatus for practicing the process of the present invention, wherein the molten salt bath is shown by cross-sectional view;
  • Figure 2 is a rear view of the embodiment of Fig. 1 ;
  • Figure 3 is a side-view of the apparatus of Fig's 1 and 2, taken along the line 3-3 of Fig. 2;
  • Figure 4 is a cross-sectional view of the molten salt bath of Fig's 1 -3, taken along the 4-4 of Fig. 1 , wherein only the drag chain is principally shown and other components have been omitted;
  • Figure 5 is an alternative embodiment for removal of insoluble inorganics from the molten salt bath, and depicts the screw conveyor arrangement
  • Figure 6 is a portion of an alternative embodiment of the apparatus shown by Fig. 1 ;
  • FIG. 7 is a schematic of a venturi scrubber which may be employed in practicing the process of the present invention.
  • Figure 8 is a cross-sectional view of yet another apparatus for practicing the process of the present invention
  • Figure 9 is an illustration of another alternative embodiment of an apparatus for practicing the process of the present invention, and is particularly suited for soil;
  • Figure 10 is a cross-sectional view of the embodiment shown in Fig.
  • Figure 1 1 is an illustration of yet another embodiment of an apparatus for practicing the process of the present invention, and is particularly suited for hospital waste.
  • Figure 12 is a schematic of another embodiment of the present invention, and is an apparatus suitable for treating solid wastes such as soil.
  • Figure 1 3 is a perspective view of a portion of a porous conveyor belt utilized in the apparatus of Figure 1 2.
  • Figure 14 is an alternative design for the apparatus of Fig. 1 2.
  • Sodium carbonate for example, is available in free flowing granular or powder forms, and since it does not tend to absorb any significant amount of moisture from the air, it can be easily added to a molten salt bath using conventional dry material feeders, such as screw or belt types. This can be significant, since alkali metal carbonate must be continuously fed to the molten salt bath if the waste being destroyed contains sulfates, halogens, phosphates, or similar moieties. Extensive testing, a portion of which is outlined below, has led to the surprising discovery that the use of alkali metal carbonate in the molten salt solution is actually superior to that which has previously been employed.
  • NaNO 3 melts at approximately 308 °C, while the melting point of Na 2 CO 3 is approximately 850 °C.
  • Na 2 CO 3 must have some appreciable degree of solubility in molten NaNO 3 at the temperatures employed for the process.
  • solubility of Na 2 CO 3 in molten NaNO 3 In order to determine the solubility of Na 2 CO 3 in molten NaNO 3 ,
  • Na 2 CO 3 was gradually added in one gram increments to 100g of NaNO 3 which had been heated to 500 °C in a steel crucible. Using this procedure it was determined that the solubility of Na 2 CO 3 in NaNO 3 was approximately 1 2% (on a weight basis).
  • solubility of salts such as NaCI in the molten mixture is also critical, since it is desired to precipitate out inorganic salts such as NaCI (or sulphates, phosphates, etc.) which form during the process.
  • NaCI is particularly significant, since polychlorinated biphenyls (PCB's) will be converted to, among other things, NaCI in the process of the present invention.
  • PCB's polychlorinated biphenyls
  • the solubility of NaCI in a molten solution comprising 90% NaNO 3 and 10% Na 2 CO 3 at 500 °C was determined to be between approximately 10% and 1 1 % by weight, which is advantageous for precipitating NaCI when the present invention is employed to destroy PCB's and similar compounds which form inorganic salts upon destruction.
  • a stirred closed laboratory reactor was charged with approximately 900 g of a salt mixture containing about 90% NaNO 3 and 10% Na 2 C0 3 (by weight), placed in a crucible furnace, and heated to 500 °C.
  • the reactor had been fitted with a reflux condenser to condense and recycle unreacted organic starting material, and a stream of air was introduced below the surface of the molten solution.
  • One ml (1 .45g) of trichlorobenzene was charged to the reactor by injecting it into the stream of air, and an immediate rise in temperature of 10 °C was observed.
  • Such a temperature increase was surprising, especially considering the amount of molten salt present in the reactor, and clearly indicates that the reaction which occurs is immediate and extremely exothermic.
  • Example 2 The reactor of Example 2 was modified so that the reactor temperature could be controlled. Ten ml of trichlorobenzene was slowly added (in a stream of air) to a molten solution having the same composition as in Example 2 over a period of 2.9 hours. The reactor temperature was held at 500 ⁇ 2 °C over this period. Analysis of the gases released during the reaction period indicated an organic destruction efficiency of greater than 98%, which confirms the fact that the reaction efficiency is greatly improved by improving the manner in which the organic waste material and the molten salt solution are contacted. While most of the trichlorobenzene is immediately destroyed, it is also necessary that the organic by-products from this initial destruction be converted into non-hazardous compounds such as CO 2 and water vapor. Thus, these organic by-products must also be contacted with the molten salt solution to ensure an efficient destruction of all organics.
  • Example 2 In order to examine the effect of omitting the carbonate from the molten solution, the experiment of Example 2 was repeated using molten NaNO 3 alone. A large amount of smoke appeared in the reflux condenser, and liquid, later identified as trichlorobenzene, was observed flowing back into the reactor from the condenser. In addition, only a small increase in temperature (less than 2 °C) was observed, further indicating that very little of the trichlorobenzene was destroyed (oxidized).
  • inorganics such as NaCI are only partially soluble in the molten solution of the present invention, and thus can generally be readily removed from the solution as they are formed.
  • Many organic wastes also contain an inorganic moiety which one desires to recover. Such is often the case with organic wastes obtained from paint manufacturing, for example, where valuable pigments are present in the "sludge" found on the bottoms of many of the vessels. While these sludges have a significant organic component, heavy metals may also be present, and it is of course imperative that they not enter the environment.
  • a paint manufacturing sludge consisting of various paint resins (alkyds, urethanes, epoxies, etc.) and inorganic pigments was charged to a reactor containing the molten solution of the present invention.
  • the molten salt (at 500 °C) consisted of approximately 90% NaNO 3 and 10% Na 2 CO 3 , by weight.
  • the resins were rapidly oxidized, and a corresponding significant increase in temperature of the molten solution was observed.
  • the reactor was opened and the molten salt solution poured off, reusable pigment solids remained.
  • a preferred method for destroying organic waste comprises intimately contacting the waste material with a molten solution of an alkali metal nitrate and an alkali metal carbonate.
  • the nitrate is sodium nitrate
  • the carbonate is sodium carbonate.
  • the molten solution should be maintained at a temperature of 450 °C or greater, and preferably about 550 °C to ensure that the reaction occurs rapidly while also ensuring that the molten solution will not decompose.
  • the molten salt solution should preferably comprise about 8 to
  • the organic waste material can be in any form, i.e., solid, liquid, or gaseous, and various contacting means may be employed.
  • the organic waste material is rapidly oxidized by the molten salt solution and converted into various reaction by-products. These by-products may include other organics, inorganic salts, CO 2 , H 2 O, and N 2 , depending upon the organic waste material being destroyed.
  • Organic by-products are further oxidized by the molten salt solution so that eventually the overall process by ⁇ products will primarily include only CO 2 , H 2 O, N 2 and inorganics.
  • the composition of the inorganics will vary greatly depending upon the type of waste material being destroyed, and may include inorganic sodium salts such as NaCI. Other possibilities include pigments (when the waste material being destroyed is paint sludge), and material such as heavy metals.
  • the reaction of the present invention can be employed for the destruction of carbonaceous materials such as aluminum pot liners. While the carbon itself does not create disposal problems, carbonaceous materials often contain other hazardous materials thereby creating a large mass of hazardous waste. For example, aluminum pot liners are predominantly carbon, however trace amounts of NaCN and NaF are also generally present.
  • the process of the present invention will oxidize both the carbon and the NaCN, and the remaining NaF will settle to the bottom of the reactor where it can later be removed. NaCN is oxidized to CO 2 , Na 2 CO 3 and N 2 , while the carbon is oxidized to CO 2 . In this fashion, the mass of the hazardous waste is almost entirely eliminated (other than the NaF).
  • the process of the present invention can be utilized to treat carbonaceous materials also.
  • catalysts can be employed to improve the destruction process, and are usually necessary for the destruction of carbonaceous materials.
  • These catalysts include any oxidation promoting heavy metal salts or heavy metal oxides, and can be used in conjunction with one another.
  • Two preferred catalysts are MnO 2 and CuO, and these are preferably employed in a ratio of 3:2 by weight, respectively.
  • These catalysts can be added to the molten salt bath at a concentration of between about 0.05% and about 0.5%, and preferably about 0.1 %. While the oxides are generally preferred, salts of the same heavy metal compounds may be employed since these salts will form their respective oxides when added to the molten salt solution.
  • Nitrate can be regenerated, however, from the nitrite thus formed merely by contacting the molten salt solution with an oxygen source such as air, thereby providing a continuous process when carbonate is also added as needed. While batch processing is certainly possible, provided a sufficient amount of carbonate and nitrate are present, continuous processing is obviously preferred.
  • the gaseous by-products from the reaction will be almost exclusively CO 2 and H 2 O. Such a gaseous mixture is relatively easy to separate, and thus can provide a relatively inexpensive source of CO 2 as an added benefit.
  • air is used to regenerate nitrate, it is preferable to employ an oxygen sensor in the gaseous by-product stream in order to maintain nitrate regeneration stoichiometry. In this fashion, the gaseous by-products will primarily include only C0 2 , H 2 O and N 2 . It is also preferred that the nitrate regeneration be performed outside of the reaction zone in which the oxidation of the organic waste material takes place if air is being used for nitrate regeneration. This ensures that the presence of the oxygen containing stream used to regenerate nitrate will not interfere with mass transfer between the molten salt solution and the organic waste being destroyed.
  • inorganic materials are only partially soluble in the molten salt solution.
  • inorganic salts such as NaCI will be formed, with the sodium ions being contributed by the sodium carbonate in the molten salt solution.
  • material such as paint sludge is to be destroyed, reusable pigments will also settle to the bottom of the molten salt solution.
  • Proper design of the apparatus in which the waste destruction takes place can ensure that these insoluble inorganics can be easily recovered and either reused or properly disposed of.
  • the waste material being destroyed may even be primarily inorganic in nature, such as the case with contaminated soil or hospital waste.
  • Fig's 1 -4 depict one preferred embodiment of an apparatus for performing the process of the present invention.
  • the apparatus shown in Fig. 1 is particularly suitable for destroying material such as paint sludge, PCB solutions, carbonaceous materials, and similar wastes.
  • the molten salt solution is maintained in molten salt bath 1 , and salt bath 1 also contains a heating means so that the salt solution may be heated to, and maintained at its proper temperature.
  • the heating means may, for example, be a gas furnace or electric heater (not shown).
  • the oxidation reaction which takes place between the molten salt solution and the waste being destroyed is extremely exothermic, and thus once the unit is operational it is normally not necessary to further heat molten salt bath 1 .
  • Heat exchangers 2 and 3 are provided at the base of columns 4 and 5, respectively, in order to remove the heat of reaction.
  • oil is pumped through exchangers 2 and 3 by pump 46 from hot oil expansion tank 47.
  • Oil coolers 48 and 49 dissipate the heat removed from columns
  • dual multi-stage packed columns 4 and 5 are positioned directly above molten salt bath 1 in fluid communication with said bath. Both columns can be packed with any suitable packing material having a high surface area, such as raschig rings, however a structured packing material such as Koch Flexipack (Koch Engineering, Wichita, KS) is preferred.
  • Reactor column 4 comprises the reaction zone in which oxidation of the waste material takes place. As will be discussed shortly however, a portion of the oxidation of the waste material might actually take place in molten salt bath 1 depending upon where the waste material is fed into the unit.
  • Regeneration column 5 is also positioned directly above molten salt bath 1 , and is utilized to regenerate nitrate in the molten salt solution from the nitrite formed by the reaction of the present invention.
  • Both reaction column 4 and regeneration column 5 preferably operate in a counter-current fashion, and submerged pump 6 transports molten salt from molten salt bath 1 to the top of both columns.
  • individual pumps could be provided for each column, however, it is preferred that a single pump be utilized, with the discharge 40 from pump 6 being split between column 4 and column 5 (see rear view shown in Fig. 2). Waste material can be fed to the unit in a number of locations, and is depicted in
  • Fig. 1 as being fed into molten salt bath 1 through feed inlet 7. It is preferred that when the material being destroyed is primarily liquid, that inlet 7 is a static mixer (shown in Fig. 1 ) such as those commonly employed. This ensures efficient contact between the waste and the molten salt.
  • reaction column 4 which is located directly above inlet 7.
  • Baffle plate 8 extending well below the surface of the molten salt, is provided in molten salt bath 1 to ensure that these gaseous by-products will only enter reaction column 4, and are not able to enter regeneration column 5.
  • These gaseous by-products will include primarily CO 2 , H 2 O, other organic compounds, and possibly N 2 depending upon the waste material being destroyed.
  • the organic by-products which rise through reaction column 4 are further oxidized as they travel upward through the column since molten salt is simultaneously passing through reaction column 4 in the opposite direction.
  • inorganics such as NaCI
  • various inorganics will remain in molten salt bath 1 , and will settle to the bottom.
  • the insoluble inorganics can be removed by a number of mechanical means, or alternatively may simply remain in molten salt bath 1 until a suitable time at which the unit can be cooled and opened for cleaning.
  • drag chain 42 having scraper blades attached thereto in a manner known in the art is provided.
  • Motor 43 drives chain 42, which picks up material which settles to the bottom of bath 1 and deposits the same in hopper 10.
  • Bottom 43 of bath 1 is also preferably sloped to form channel 44 into which insolubles will collect for easier removal.
  • Screw conveyor 9 shown in Fig. 5 may alternatively be provided in order to remove inorganics which settle to the bottom of molten salt bath 1 , provided that the bottom 41 of molten salt bath 1 is appropriately sloped. The inorganics are removed along the path of screw conveyor 9 in the direction shown, and are deposited into waste hopper 10.
  • any of a number of alternative mechanical means may be utilized to remove the organics from molten salt bath 1 .
  • the nitrate contained in the molten salt solution is converted into the corresponding nitrite during the course of the oxidation reaction.
  • the molten salt solution containing nitrite is pumped to the top of regeneration column 5.
  • air is fed through air inlet 1 1 located near the base of regeneration column 5.
  • the oxygen contained in the air will thus regenerate nitrate from nitrite, and the molten salt solution now containing the regenerated nitrate will fall back into molten salt bath 1 .
  • an oxygen sensor may be placed in the overhead gas stream from regeneration column 5, and this sensor will ensure that a stoichiometric amount of oxygen is being provided to regeneration column 5. In this fashion, pure N 2 will be produced by regeneration column 5.
  • pure oxygen may be utilized instead of air in order to regenerate the nitrate from nitrite, which would permit regeneration column 5 to be reduced in size.
  • oxygen spargers can be placed in molten salt bath 1 , thereby eliminating entirely the need for a regeneration column. By placing spargers in the bath, regeneration of nitrate from nitrite takes place in the bath itself. The mass transfer inhibiting dilution discussed previously does not occur since, if properly controlled, all of the oxygen injected into the bath is consumed in the regeneration reaction.
  • the overhead gases from both reaction column 4 and regeneration column 5 can be combined, and optionally pass through scrubber 1 2 (entering near its base as shown in Fig. 2) in order to ensure that no organics remain in these vent gases.
  • Scrubber 1 2 can be of any typical design utilized for this purpose.
  • Induced draft fan 1 3 may also be employed to maintain a negative pressure on reaction column 4, regeneration column 5 and optional scrubber 1 2, thereby ensuring that any leakage will be inward.
  • Induced draft fan 13 (in fluid communication with outlet 45 of scrubber 1 2) also ensures that the gaseous by-products will eventually be vented to the atmosphere. Since the overhead gases from reaction column 4 and regeneration column 5 will obviously be at an elevated temperature, heat exchangers may also be provided to recover some of this heat and even preheat the air being fed to regeneration column 5.
  • organic waste material may be optionally fed to a scraped-surface still in which any solvents in the waste material may be removed through simple distillation.
  • the heat needed for this distillation may even be provided by the heat exchangers previously mentioned for removing the heat of reaction from the oxidation of waste material.
  • the means by which the waste material to be destroyed is fed into the unit will vary greatly depending upon the type of material one wishes to destroy, however a simple feed pump will suffice for most liquid wastes.
  • FIG. 6 An alternative design for this process unit is shown in Fig. 6, wherein the reaction column and regeneration column previously discussed are combined into a single structure.
  • the overall configuration of the unit is essentially the same other than this distinction.
  • Single packed column 1 6 comprises lower reaction section 1 7 and upper regeneration section 1 8.
  • Molten salt is pumped from molten salt bath 1 by means of pump 6 to the top of upper regeneration section 18.
  • a portion of a typical distributor arrangement is shown in Fig. 6, however any of a number of alternative configurations can be employed.
  • the molten salt enters regeneration section 1 8 through perforated distributor pipe 70. Overhead gases from regeneration section 18 exit through vent line 25, and may one again be directed to an optional scrubber.
  • Packing 72 is supported by grid 73 which permits both upflowing vapors and downflowing molten salt to pass through.
  • the molten salt solution flows downward through regeneration section 18, and is contacted with air, or alternatively oxygen, which has been fed into the base of regeneration section 1 8 (below grid 73) through air inlet 1 1 .
  • any nitrite contained in the molten salt solution is contacted with the upflowing air, and nitrate is thus regenerated.
  • the molten salt solution continues to flow downward through grid 73, and thus enters lower reaction section 1 7.
  • the molten salt solution flows countercurrent to either the waste material being destroyed or the gaseous reaction by-products, depending upon the feed location for the waste material.
  • the organic waste material may be fed into either the base of lower reaction section 1 7, or alternatively directly into molten salt bath 1 which is located beneath lower reaction section 1 7. In this manner, the organic waste material is oxidized by the down flowing molten salt solution, as previously discussed.
  • vent line 24 any inorganics, such as inorganic salts or pigments will accumulate in molten salt bath 1 .
  • the vent gases exit through vent line 25, and may be combined with those from vent line 24 for further treatment as needed.
  • a spray scrubber or venturi scrubber may be employed in place of the packed columns for gas-molten salt contacting. Either of these apparatus may replace the reaction column and/or the regeneration column, however they are generally not as efficient as packed columns.
  • FIG. 7 depicts a typical venturi scrubber 33 which may be utilized in place of the reaction column and/or the regeneration column.
  • Venturi scrubber 33 comprises gas inlets 34, liquid inlet 36 and gas/liquid outlet 37.
  • the molten salt solution is fed through liquid inlet 36, contacts the gaseous material entering through gas inlet 34, and the resulting mixture is dispersed and mixed by nozzle 38.
  • the gaseous material entering gas inlet 34 may be the organic waste material to be destroyed, gaseous reaction by-products, or air (or oxygen) which is being utilized to regenerate nitrate.
  • the molten salt solution and gaseous components entering venturi scrubber 33 are carried into separation chamber 39 wherein both the gaseous by-products and molten salt solution exit through outlet 37.
  • venturi scrubber 33 and spray scrubbers offer viable alternatives for ensuring intimate contact between the molten salt solution and the organic waste material to be destroyed (or alternatively the air being used to regenerate nitrate).
  • a stirred tank reactor may replace the venturi scrubber for any of the uses described herein for venturi scrubbers. Such reactors may, for example, be of the type described in the chapter entitled Gas-Liquid Reactors, of Mass Transfer Operations, by Traybal, and in Perry's Chemical Engineers' Handbook, pages 4-24 to 4-27 (6th Ed.).
  • FIG 8 shows yet another embodiment of an apparatus suitable for performing the process of the present invention.
  • molten salt bath 1 is provided for maintaining the molten salt solution at the desired temperature.
  • Bath 1 is placed in fluid communication with angled reaction pipe 50, and a means (such as pump 90) is provided for pumping molten salt from molten salt bath 1 into angled reaction pipe 50 through salt inlet 51 .
  • Salt outlet 52 is also provided, and is located along the length of angled reaction pipe 50, just prior to solids exit 53 of reaction pipe 50. In this fashion, the molten salt solution will not fill the entire length of angled reaction pipe 50, thereby ensuring that a vapor space 54 will be present in the vicinity of solids exit 53 of reaction pipe 50.
  • Hollow cylindrical shaft 55 is contained within reaction pipe 50, and screw 56 is attached around the circumference of shaft 55.
  • Shaft 55 is rotatably attached to end wall 57 of reaction pipe 50, and thereby permits screw 56 to rotate within reaction pipe 50.
  • Rotation of screw 56 is accomplished merely by providing a means for rotating shaft 55, such as an electric motor. If a diesel engine is employed for this purpose or for electricity generation for the process, the diesel exhaust can be directed down the length of shaft 55.
  • shaft 55 may actually comprise concentric tubes 58 and 59, with inner concentric tube 58 open at the end of shaft 55 which is rotatably attached to end wall 57.
  • the diesel exhaust flows along the length of shaft 55 through inner concentric tube 58, and then returns in the opposite direction through outer concentric tube 59 after the exhaust has travelled to a point adjacent end wall 57.
  • the purpose of running the diesel exhaust through shaft 55 is to provide a means for economically heating the molten salt solution contained in reaction pipe 50.
  • the organic waste to be destroyed enters reaction pipe 50 through inlet 60, located beneath the surface of molten salt contained within pipe 50, where it contacts the molten salt solution contained therein.
  • the organic material is immediately oxidized and gaseous by-products flow along angled reaction pipe 50 with the rotation of screw 56 until they enter vapor space 54.
  • complete destruction of any organic material present in the waste can be assured, since the gaseous by-products remain in contact with the molten salt until they reach vapor space 54.
  • Gaseous by-products which enter vapor space 54 exit reaction pipe 50 through vent 61 , and may thereafter be vented to the atmosphere.
  • a packed column 62 similar to those described previously may be placed in fluid communication with vent 61 in order to further oxidize any organics remaining in the gaseous by-product stream.
  • Molten salt solution may also be pumped into packed column 62, in order to oxidize any organic vapors present in the stream being vented from reaction pipe 50.
  • the operation of packed column 62 will not be discussed in detail here, since its operation is identical to that of the reaction columns previously discussed.
  • the spray scrubber or venturi scrubber previously discussed may also be employed in place of packed column 62 if desired.
  • an induced draft fan may be placed in fluid communication with the gas outlet 64 from packed column 62 to provide a slight negative pressure throughout the system, thereby ensuring that the gaseous by-products will be drawn through packed column 62.
  • sparger 65 may be placed in molten salt bath 1 . Air or pure oxygen is fed through sparger 65, and thereby regenerates nitrate within the molten salt solution. The air or oxygen entering through the sparger will also act to cool the molten salt solution as needed. Additionally, a heat exchanger may be placed between salt outlet 52 and molten salt bath 1 in order to remove the excess heat of reaction.
  • Wire brushes 66 act to clean the inside surface of reaction pipe 50, ensuring that the insoluble inorganics are carried along the length of reaction pipe 50 by screw 56 as shaft 55 rotates. In this fashion, these insoluble inorganics are moved along the length of reaction pipe 50 and eventually urged towards solids outlet 53. Since the liquid level 68 of the molten salt solution within reaction pipe 50 lies below solids outlet 53, primarily only solids will be discharged into solids outlet 53. Although a small amount of the molten salt solution will exit through solids outlet 53, carbonate and nitrate can be added to the molten salt solution as needed to replace that which is lost.
  • Figures 9 and 10 depict a modification of the apparatus of Fig. 8, and is particularly suited for materials such as hospital waste and contaminated soil.
  • an alkaline material such as an alkali metal carbonate (e.g. CaO or MgO) or lime
  • alkali metal nitrate can accomplish the desired oxidation of organics.
  • the preferred alkaline material is sodium carbonate due to its water solubility, however even lime is acceptable for some soils.
  • the soil or hospital waste is pre-mixed with either a dry blend of the carbonate (or lime) and nitrate, or a water solution containing the carbonate and nitrate.
  • the pre-mixed waste/salt blend can be accomplished in a concrete mixer or similar device. It is preferred that the pre-mixed waste/salt blend contain approximately 20% moisture, and this can be accomplished by first adding the nitrate to a water and carbonate or lime slurry. The resulting solution is then mixed with the solid waste material in a ratio of approximately five times the stoichiometrically required amount. It has been found that when this organic waste/salt mixture is heated to at least about 350° C, and preferably at least about 450° C, the desired oxidation takes place and the organic component of the waste is thereby destroyed. Since the reaction is exothermic, it is also possible to recover heat from the process, however significant amounts of heat can only be recovered if there is a large amount of organic material present in the soil or hospital waste.
  • a shaft 55, with attached screw 56, preferably having wire brushes 66 attached thereto is provided.
  • shaft 55 is placed within reaction trough 80, and the lower portion of screw 56 will rest against the inner surface of reaction trough 80.
  • a vapor space 81 is also provided above screw 56. This can be accomplished by providing a rectangular enclosure 82 above reaction trough 80.
  • alternative designs equivalent to this structure may be employed, and the apparatus shown in Fig's 9 and 10 is merely a preferred embodiment.
  • the pre-mixed organic waste/salt mixture is added through inlet 83 near one end of reaction trough 80.
  • feed means may be employed and may for example be a hopper in fluid communication with inlet 83 or a rotary air-lock type feeder. Since shaft 55 is once again rotatably attached to end 84 of reaction trough 80, as shaft 55 is rotated, the solid mixture is carried along the length of reaction trough
  • a salt jacket 85 extends along the length of reaction trough 80, and thereby provides heat to the dry mixture contained therein (of course alternative means for heating reaction trough 80 could be employed. It is preferred that the unit is operated such that the mixture achieves the desired temperature prior to reaching the end of reaction trough 80.
  • Means for heating the salt jacket is also provided, and may, for example, be electric Firebar heaters 86 (manufactured by Watlow Electric Manufacturing, St. Louis, Missouri) placed along the length of salt jacket 85, thereby enabling the salt contained in the salt jacket to be melted.
  • Molten salt bath 1 is once again provided, and is placed in fluid communication with salt jacket 85, and heaters 79 are also contained therein.
  • a means for pumping the molten salt solution from molten salt bath 1 is provided, and may for example be pump 87.
  • Pump 87 preferably pumps molten salt to the top portion of salt jacket 85, and it is preferred that salt outlet 78 (see Fig. 10) be similarly located.
  • Salt inlet 77 is also located accordingly (see Fig. 9). This ensures that the salt will not drain from salt jacket 85 when pump 87 is turned off. It is also preferred that the flow of salt through salt jacket 85 be countercurrent to the movement of solids through reaction trough 80.
  • reaction trough 80 As the pre-mixed organic waste/salt mixture is carried along the length of reaction trough 80, the mixture is heated thereby causing the oxidation reaction to occur. The gaseous by-products of this reaction enter vapor space 81 and are carried through vent 88. Once again an induced draft fan may employed to ensure that the gaseous by-products are removed.
  • the solid inorganic material is carried along reaction trough 80, and eventually is urged into solids outlet 67. If, for example, contaminated soil is being treated, the material ejected through solids outlet 67 will comprise primarily the treated soil, and will be essentially free of all organics. In the case of soil, another advantage of this process is that the addition of lime and nitrates to the soil has added benefits when, for example, the treated soil is later utilized as fill, as these components act as soil fertilizers.
  • the gaseous by-products leaving through vent 88 may contain some organics, depending upon the nature of the organic waste being treated, once again a packed column or other means for oxidizing these organics may optionally be provided.
  • the design of these units is identical to that described previously for the angled reaction pipe design, and will not be dealt with in detail here.
  • the molten salt bath of Fig's 9 and 10 may even be employed for this purpose, in addition to its heating function.
  • a scrubber of the type known to those skilled in the art if the organic gaseous by-products are such that they can be effectively removed in this manner.
  • FIG. 1 1 depicts yet another embodiment for practicing the process of the present invention, and is particular suitable for hospital waste and the like.
  • molten salt bath 101 is provided, and any suitable means for heating bath 101 (such as those described previously) is also provided.
  • This heating means could, for example, comprise heat exchanger tubes passing through bath 101 , or even an electric heating element placed within bath 101 .
  • the destruction reaction takes place in perforated or screen drum 102 which is rotatably secured within molten salt bath 101 . Rotation of drum 102 may be accomplished, for example, by motor 104 attached thereto.
  • Drum 102 is typically of the type commonly used in degreasing or deburring small parts, such as drums manufactured by the Ransohoff Co. of Hamilton, Ohio.
  • Perforated drum 102 permits molten salt to enter its interior, and as shown in Fig. 1 1 the lower portion of drum 102 is positioned slightly below salt level 1 1 0. Spiral ridges 106 are provided along the interior of drum 102 in order to ensure that solid material contained therein is moved along the length of drum 102 as it is rotated.
  • the material to be destroyed is fed into hopper 103, from which it enters drum 1 02 through feed chute 1 1 1 .
  • the organic portion is immediately destroyed in the same fashion as before. Gaseous by-products enter vapor space 1 1 2, and eventually escape through vent 105.
  • a packed column or other means e.g. a venturi scrubber
  • salt from molten salt bath 101 be utilized for this purpose in the manner described previously.
  • the solid inorganic portion of the waste remaining in drum 102 is carried along the length of drum 102 by spiral ridges 106, thereby complete destruction of any organic material.
  • these ridges are typically arranged, as is well-known in the art, such that the solids are deposited into discharge chute 107 and deposited in waste hopper 108.
  • this latter feature may be eliminated.
  • the apparatus would merely be opened periodically to remove any solids accumulating at the end of drum 102 or in bath 101 .
  • sparger 109 is preferably provided in bath 101 .
  • air or oxygen may be pumped into bath 101 to regenerate nitrate.
  • a regeneration column or the like (as described previously) may optionally be employed for the same purpose. Since it is likely that some of the molten salt may be carried out with the solid inorganics, and since a portion of the carbonate present in the molten salt may be consumed as described previously, it will also be necessary to replenish the molten salt periodically. This could be accomplished through feed chute 1 1 1 , although other means may certainly be employed.
  • Figures 1 2 - 14 depict yet another apparatus particularly suited for destroying material such as hospital waste and contaminated soil.
  • the apparatus shown in these figures is preferably employed with the process described for the apparatus of Figures 9 & 10, using a blend of an alkaline material and an alkali metal nitrate to accomplish the desired oxidation of organics.
  • the entire apparatus of Figure 1 2 or Figure 14 may be provided in any suitable enclosure 1 1 2.
  • the pre-mixed waste/salt mixture is added through inlet 101 , and thereafter falls upon a porous, continuous conveyor belt 102. While the construction of porous conveyor belt 1 02 can vary, one preferred design is shown by Figure 1 3.
  • the conveyor shown in Figure 1 3 is comprised of connecting rods 1 25 and transverse elements 126, each of the transfers elements having convolutions which interdigitate with adjacent convolutions so that connecting rods 1 25 may penetrate the adjacent convolutions thereby permitting the transverse elements to rotate about the connecting rods.
  • These porous conveyors, or grate-type conveyors are commonly employed in various industries for such uses as bottle washing. Bottles can be placed atop the conveyor and water cascaded down upon the bottles for washing purposes. The water is there then permitted to pass through the conveyor to a suitable collection system.
  • Conveyor belt 1 20 is further defined by upper flight 1 30, and lower flight
  • first and second sprocket wheels 104 and 103 respectively. Rotation of first and second sprocket wheels will thereby cause belt 1 20 to move, preferably from the first wheel towards the second wheel, as shown in Fig. 12.
  • the conveyor belt moves atop an upper planar surface, namely support plate 1 07, and thus the waste/salt mixture will loosely rest within compartments 1 27 atop, and retained by, plate 107.
  • the porus conveyor employed has a height of approximately one half to three quarters inches, and provides compartments 1 27 having a volume of approximately 0.5 cubic inches.
  • porous conveyor belt 1 02 is driven by sprocket wheels 1 03 and 104.
  • These wheels are of a typical construction for such a use, and the sprockets are not shown in Figures 1 2 and 14 for the sake of simplicity.
  • a plurality of sprocket wheels may also be provided to ensure uniform and smooth movement of the conveyor, with successive sprocket wheels connecting to one another by a common axle.
  • One or more of the sprocket wheels are mechanically driven, and the remainder are free spinning.
  • second sprocket wheel 1 03 preferably comprises a substantially solid drum of substantially the same width as belt 102.
  • Radiant heater 105 is positioned above porous conveyor 102, and heats the waste/salt mixture from above. Radiant heater 105 may be powered by any suitable means, including gas, oil, electricity, or even molten salt. Since support plate 107 is preferably of a conductive material such as metal, a plurality of heaters 106 are also preferably provided beneath support plate 107. These may likewise be fired by any suitable means such as those previously described, including molten salt. In this manner, the salt/waste mixture, which preferably is soil and the appropriate salt combination, will be heated from both above and below. This will ensure a relatively uniform temperature throughout the mixture, and will quickly initiate the oxidation reaction.
  • porous conveyor 102 passes across support plate 107 carrying the waste/salt mixture in its compartments 1 27, the conveyor passes around sprocket wheel 103 to reach lower support plate 108.
  • substantially arcuate reversing guide 109 is provided adjacent sprocket wheel 103.
  • belt 102 will pass between the second sprocket wheel and the reversing guide, and the mixture will be retained within the compartments by the guide and the solid, drum-shaped sprocket wheel.
  • the conveyor passes around sprocket wheel 1 03, however, some mixing of the waste/salt mixture will occur as this mixture is rotated through 1 80 degrees.
  • lower flight 1 31 rides atop lower planar surface, or lower support plate, 108, and the mixture is retained within the compartments 1 27 by support plate 108.
  • a plurality of heaters 106 may be provided beneath lower support plate 108 in order to continue heating of the reacting mixture.
  • radiant heat from heaters 106 located above lower support plate 108 will provide further heat to the mixture.
  • Conveyor 102 passes along lower support plate 108 until reaching a point preferably near sprocket wheel 104 where lower support plate 108 terminates. At this point, the solid inorganic material remaining is discharged from compartments 1 27 of conveyor 102, and falls into solids outlet 1 1 0.
  • vent 1 1 1 is provided.
  • an induced draft fan may also be employed to be ensured that the gaseous by-product are removed.
  • the previous means described for further treating the gaseous by-products leaving through vent 1 1 1 may once again be employed in the designs of Figure 1 2 and 14, including the use of molten salt to remove any organic material remaining in the gaseous by-products.
  • Figure 14 depicts a modification of the apparatus of Figure 1 2, and provides for an increased residence time for the waste/salt mixture.
  • the apparatus of Figure 14 generally comprises a plurality of porous conveyor belt systems, with the waste/salt mixture constantly reversing directions as it moves within each belt.
  • Support plate 1 22 has also been modified, as the plate terminates a predetermined distance from second sprocket wheel 1 21 .
  • the sprocket wheels employed preferably do not extend across the entire width of belt 102. Rather, sprocket wheel is preferably only a fraction of the width of belt 102, and must merely be thick enough to support belt 102.

Landscapes

  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Soil Sciences (AREA)
  • Toxicology (AREA)
  • Thermal Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Business, Economics & Management (AREA)
  • Emergency Management (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treatment Of Sludge (AREA)

Abstract

Un procédé qui permet de détruire la partie organique de déchets, consiste à mettre une solution de sels fondus en contact avec ces déchets. On décrits aussi l'appareil, utilisé avec ce procédé, qui comporte une cuve pour sels fondus et plusieurs dispositifs permettant d'obtenir le contact nécessaire. On décrit de plus un procédé qui utilise des substances alcalines et des nitrates mélangés pour détruire la partie organique de déchets solides, ainsi qu'un appareil qui permet de le mettre en ÷uvre.
PCT/US1994/003912 1993-04-08 1994-04-08 Procede et appareil destines a detruire des dechets organiques et contenant des hydrocarbures WO1994023802A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
NZ265199A NZ265199A (en) 1993-04-08 1994-04-08 Process for destruction of organic waste by contacting with a molten metal nitrate and alkali metal carbonate salt solution
AU65572/94A AU696437B2 (en) 1993-04-08 1994-04-08 Process and apparatus for destroying organic and carbonaceous waste

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US4575593A 1993-04-08 1993-04-08
US08/045,755 1993-04-08

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5817504A (en) * 1996-11-01 1998-10-06 Dana Corporation Method and apparatus for accelerated decomposition of petroleum and petro-chemical based compounds within filter media
US5854012A (en) * 1997-12-17 1998-12-29 Dana Corporation Composition, method and apparatus for safe disposal of oil contaminated filter
WO2009048439A1 (fr) * 2007-10-10 2009-04-16 Sergiy Yuriyovych Stryzhak Procédé de transformation de déchets industriels ou ménagers et installation destinée à sa mise en oeuvre
US10888200B1 (en) 2017-11-08 2021-01-12 Sympateco, Inc. Shower basin
USD913463S1 (en) 2017-11-08 2021-03-16 Sympateco, Inc. Shower basin
USD913462S1 (en) 2017-11-08 2021-03-16 Sympateco, Inc. Shower basin
CN113025286A (zh) * 2021-03-11 2021-06-25 北京工业大学 钠基二元熔盐高温传热蓄热工质
CN113292969A (zh) * 2021-05-12 2021-08-24 北京工业大学 一种具有高潜热的中高温混合熔盐蓄热体系和制备方法
CN114717015A (zh) * 2022-04-05 2022-07-08 昆明理工大学 有机废物协同熔盐制炭基材料联产燃气的方法与装置

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FR2331759A1 (fr) * 1975-11-14 1977-06-10 Inst Po Metalloznanie I Tekno Four de fusion
US4469661A (en) * 1982-04-06 1984-09-04 Shultz Clifford G Destruction of polychlorinated biphenyls and other hazardous halogenated hydrocarbons
US4497782A (en) * 1982-10-28 1985-02-05 S. Garry Howell Method for destroying toxic organic chemical products
JPS6057299A (ja) * 1983-09-09 1985-04-03 三菱重工業株式会社 汚染された金属材料の洗浄方法
US4552667A (en) * 1984-06-25 1985-11-12 Shultz Clifford G Destruction of organic hazardous wastes
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Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5817504A (en) * 1996-11-01 1998-10-06 Dana Corporation Method and apparatus for accelerated decomposition of petroleum and petro-chemical based compounds within filter media
US5958759A (en) * 1996-11-01 1999-09-28 Dana Corporation Composition method and apparatus for safe disposal of oil contaminated filter media
US6121039A (en) * 1996-11-01 2000-09-19 Lasky; William M. Composition, method and apparatus for safe disposal of oil contaminated filter media
US6316249B1 (en) 1996-11-01 2001-11-13 Dana Corporation Composition, method and apparatus for safe disposal of oil contaminated filter media
US5854012A (en) * 1997-12-17 1998-12-29 Dana Corporation Composition, method and apparatus for safe disposal of oil contaminated filter
US20100251944A1 (en) * 2007-10-10 2010-10-07 Sergiy Yuriyovych Stryzhak Method for Processing Industrial and Domestic Wastes
WO2009048439A1 (fr) * 2007-10-10 2009-04-16 Sergiy Yuriyovych Stryzhak Procédé de transformation de déchets industriels ou ménagers et installation destinée à sa mise en oeuvre
US10888200B1 (en) 2017-11-08 2021-01-12 Sympateco, Inc. Shower basin
USD913463S1 (en) 2017-11-08 2021-03-16 Sympateco, Inc. Shower basin
USD913462S1 (en) 2017-11-08 2021-03-16 Sympateco, Inc. Shower basin
CN113025286A (zh) * 2021-03-11 2021-06-25 北京工业大学 钠基二元熔盐高温传热蓄热工质
CN113292969A (zh) * 2021-05-12 2021-08-24 北京工业大学 一种具有高潜热的中高温混合熔盐蓄热体系和制备方法
CN113292969B (zh) * 2021-05-12 2022-03-15 北京工业大学 一种具有高潜热的中高温混合熔盐蓄热体系和制备方法
CN114717015A (zh) * 2022-04-05 2022-07-08 昆明理工大学 有机废物协同熔盐制炭基材料联产燃气的方法与装置
CN114717015B (zh) * 2022-04-05 2023-10-24 昆明理工大学 有机废物协同熔盐制炭基材料联产燃气的方法与装置

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AU6557294A (en) 1994-11-08
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