US2824058A - Method for the continuous self-sustaining flameless oxidation of combustible materials - Google Patents

Method for the continuous self-sustaining flameless oxidation of combustible materials Download PDF

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US2824058A
US2824058A US397959A US39795953A US2824058A US 2824058 A US2824058 A US 2824058A US 397959 A US397959 A US 397959A US 39795953 A US39795953 A US 39795953A US 2824058 A US2824058 A US 2824058A
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water
reaction zone
combustible
feed
reactor
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US397959A
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Frederick J Zimmermann
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STWB Inc
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Sterling Drug Inc
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C02F11/08—Wet air oxidation
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/12—Combustion of pulp liquors
    • D21C11/14—Wet combustion ; Treatment of pulp liquors without previous evaporation, by oxidation of the liquors remaining at least partially in the liquid phase, e.g. by application or pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F01K3/18—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
    • F01K3/188—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters using heat from a specified chemical reaction
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S159/00—Concentrating evaporators
    • Y10S159/24—Critical

Definitions

  • the present invention relates to a method for ⁇ continuously oxidizing combustible materials with an oxygenating gas in an aqueous dispersion under conditions suchthat ⁇ the oxidation process is self sustaining and generates heat energy in excess of that required to maintain the ameless oxidation. More particularly, the present invention is characterized by feeding a combustible material dispersed in liquid water into a reaction zone which contains a large quantity of combustible material andrliquid waterand inducing a nameless oxidation while maintaining they quantity and concentration of the combustibleinaterial in the reaction zone substantially constantad oxidizing only at the rate at which fresh oxidizable' material dispersed in water is fed to the zone.
  • the invention also relates to the continuous transformation ofv mass 'energy latent in combustible material
  • it is a purpose of this invention to provide a process for continuously oxidizing combustible materials dispersed in liquid water which includes the steps of continuously passing a combustible material dispersed in liquid water and an oxygen-containing gas into a reaction zone while maintaining in said zone the concentration of combustible material dispersed in the liquid water sufficiently high to oxidize all the combustible material at the 'rate at which it is fed into the reaction zone.
  • the upper limit of the concentration of ⁇ combustible material in water is that at which the amount of energy liberated 4-rby tbeoxidation is insufficient to vaporize all bustible materials dispersed in liquid water by the maintenance'of a, desired concentration of combustible ma- ⁇ terial in a reaction zone.
  • non-condensible i. e., carbon dioxide, oxygen, nitrogen,
  • This process for the generation of heat energy permits complete combustion of the fuel; eliminates conventional metallic thermal exchange barriers; permits the use of dilute aqueous combustible substances, such as carbonaceous wastes, as fuel; eliminates the problem of expansion of gases during combustion; and, permits maintaining combustibles in liquid phase above their ignition temperatures whereby theirV llameless oxidation is accomplished.
  • the invention is particularly characterized by the fact that it is unnecessary to reduce the volume of the raw efuents containing the combustible materials as by proF edures such as dehydration, evaporation, orl precipitation.
  • proF edures such as dehydration, evaporation, orl precipitation.
  • a ilameless combination of oxygen with combusible 'matter takes place in the presence of the liquid water of the effluent with' the accompanying liberation of heat energy.
  • the application of this heat energy results in a power cycle.
  • the cycle contemplates the oxidation of the dilute aqueous oxidzable substances in their natural or dilute liquid state for the purpose of converting them to heat and mechanical energy.
  • My process is limited to the self-sustaining oxidation of the oxidizable materials in aqueous dispersion carried out at flame ⁇ less combustion while the oxidizable materials are dispersed in liquid water, which water is maintainedv at least partially inthe liquid phase in the reactor.
  • oxidation or combustion of oxidizablev materials in the dry state such as in a furnace in which the temperature of self-sustaining oxidation is several hundred degrees -above the range of the present process andl little or no liquid water is present.
  • the invention also makes it not only possible but desirable in instances to generate steam energy from low grade powered fuels by first mixing such fuel in a relatively large quantity of water.
  • Such a process for the conversion of the potential heat energy in the fuel to useable steam energy has several important advantages.
  • the kernel of the problem is' the fact that'heretofore no process has ever beendeveloped by which the waste efuents couldbe utilized as a fuel without at least partial concentration' of the liquor containing the carbonaceous substances before converting the carbonaceous substances to heat energy.
  • the usual way of'obtainingenergy from a dilute aqueous waste involves evaporation of water. For this evaporated water the' latent heat of vaporization must'be suppliedandis lost in the process.
  • This invention eliminates, for the rst time, these heat energy wasting steps. Instead of attemptingto refine the steps of 'these' standard processes, to render them more efficient( this invention eliminates a ⁇ major portion of the energy wasting steps, whereby'th'e energy produc ing stepis permitted to predominate, rendering the overall process. highly efficient.
  • My invention.' not only makes 4 the process self sustaining but changes the balance between energy generation and cons'urn'pti'onV t'o" suclr an' extent that the process is capable of producing substantial quantities of energy in excess of that required to sustain the oxidation reactions'
  • the quantity of the oxygen-containing gas requiredy is preferably that theoretically required toconverte', allJ of the combustible matter in the aqueous disp,ersion toits end products, such as carbon dioxide, water, nitrogen, sulfates, nitrates, carbonates, phosphates, et cetera, or slightly in excess of such' amount, which is readily. determinable by standard methods from the analysis ofith'e combustible material and its oxygen demand.
  • the single ligure is a schematic flow diagram illustrating one way of practicing my invention as a power generating procedure, utilizing waste sulphite pulp mill liquor.
  • the flow sheet details the process as applied to a supply of 300 gallons per minute of ordinarywaste sulphate'liquor.
  • the said'liquor is pumped'underapressure of 1400 to l500'poundsfper square inchgaugey into aL reactor vessel which may beaverticaltower, constructed' to withstand pressuresvup to, for example, ZOO-atmospheresi Air or any suitablemixture off gases-containing oxygen is compressed and passedv throughintericoolersin heatexchange relation with cold water, if a large supply' ofh'ot*wa'tersdesired for related plant'purposes. ⁇
  • the pressure in' the reactor is suicient to maintain substantially all ofthe water in the liquid phase.
  • the temperature in the reactor which may, in starting up, require heating to the ignition temperature of any particular fuel under the pressure employed, maintains itself generally in a range above 500 degrees Fahrenheit and the critical temperature of water, depending upon the proportions of oxygen to combustible substance in the feed. In the instance of sulphite liquor a temperature of 260 degrees centigrade 'to 315 degrees centigrade is readily maintained.
  • An oitake is provided from the reactor to a first separator from which xed gases including nitrogen and carbon dioxide, and steam in desired amount are ilashed through a topping turbine for power generation purposes.
  • the exhaust from the said turbine may be passed through a heat exchanger to supply progress steam for a related plant operation and thence to a second separator.
  • additional steam is dashed, at a temperature of ⁇ about 300 degrees Fahrenheit, accompanied by the fixed gases, through an exhaust turbine to generate further power.
  • From said second separator the water not flashed is led through a throttling valve to a third separator and process steam flashed off for related plant use.
  • the liquid water remaining, having a temperature of about 275 degrees Fahrenheit, may be used as hot water in related plants.
  • the iirst step toward initiating the process is charging the reactor, at least partially with liquor.
  • This charge of liquor is then heated by a suitable means such as an oil ring as to a temperature of 500 to 550 degrees Fahrenheit.
  • the heating of the liquor in the reactor is stopped and compressed air supplied to the reactor.
  • the admission of the compressed air to the reactor initiates Athe oxidation of the combustible substances, and thereafter,
  • reaction is self sustaining, requiring no ⁇ further external heat.
  • reactor design and availability of fuels may warrant the application of external heat or the ⁇ injection ⁇ of fuel values into the aqueous oxidizable materials being processed.
  • the air may be admitted through a single port at the bottom of the reactor but preferably it is admitted through a dispersion head toeffectintimate 4dispersion of the air through the liquor. y The air may even be admitted at additional points along the reactor, if such is desired.
  • the primary object is to geta thorough dispersion or diffusion of the air throughout the liquor to assure oxidationv of each of the carbon-containing molecules or other combustible substance in the liquor. ⁇ A plurality of interconnected reactorzones may be employed if desired.
  • the oxidation of the carbon compounds results in the degradation of the complex carbon-containing molecules to the end products ofl water and carbon dioxide.V
  • Thel initialhheat supplied to the starting charge of raw waste liquor is essential because the oxidation process will not start unless the liquor is heated to or above the autogenetic 4oxidation temperature ofthe carbonaceous or other combustible materials. 'Provided the liquor is maintained under a pressure suicientto keep the water substantially in the liquid phase, ⁇ this ignition temperature has been found to be a minimum of approximately 160 degrees centigrade,
  • temperatures above 191 75 degrees centigrade areused and the optimum'range is" such as air or otherwise desirably diluted oxygen, prefer-v ably that amount theoretically necessary to convert all of the carbon in the combustible substance to carbon dioxide.
  • the liquor When the liquor leaves the reactor, it enters the first of a series of separators or flash chambers.
  • the pressure is lowered a predetermined amount, thus, the tiash chambers are in effect a series of pressure reduction steps.
  • the pressure In the first chamber the pressure is reduced suiiiciently to release as an elastic uid the lixed ⁇ gases such as nitrogen and carbon dioxide, together with a desired quantity of high-pressure water vapor.
  • steam is released at varying pressures as desired.
  • the precise procedure by which the process steam is made available is immaterial to the principle of my invention,- so long as the steam is flashed after the oxidation reaction has been completed.
  • the heat generated by the oxidation of the combustible materials is in excess of that necessary to heat the liquor entering the reactor to a temperature at which the autogenetic oxidation of the raw liquor will occur. Because of this autogenetic heat, once the reaction has been established as a source of heat energy, the liquor may even be introduced into the reactor at room temperature, that is, about 70 degrees Fahrenheit.
  • the heat generated by the oxidation reaction already taking place in the ⁇ reactor is suiiicient to raise the temperature of the incomingy liquor to the' combustion temperature of the carbonaceous or ⁇ other combustible material therein present, such as sulphur.
  • the incoming liquors may be preheated by means of a heat exchanger utilizing the effluent discharged from the last ilash chamber after the release of the fixed gases and process steam.
  • the effluent discharged from the last ash chamber is at an elevated temperature of about 200 degrees Fahrenheit.
  • liquors are normally discharged from the pulping process at approximately degrees Fahrenheit and may be supplied to the reactor at this temperature, my process will operate efficiently when supplied with liquor cooled to normal room temperature, that is, approximately 70 degrees Fahrenheit.
  • theetiluent discharged from the ash chamber may be utilized as a source of heat by means of a heat exchanger for heating these incoming liquors. In this manner, less of the heat generated in the reactor needs to be utilized to raise the fresh liquor to the temperature at which autogenetic oxidation will occur. This heat energy may be conserved to develop greater quantities of process steam. Heat may also be conserved by insulating the reactors and piping.
  • the oxidation becomesyself sustaining.
  • the liquori isheatedtby the' energy given olf in the oxidationreac-y tion.
  • the quantity of liquor vaporized in' theY reactor zoiie is determined by the pressure maintainedtherein. The. energy absorbed by this vaporization produces useful process steam and, as such, the energy is productive of a valuable end-product of the process rather than absorbed by an essential operating requirement of the process itself.
  • the total amount of British thermal units abstracted from the heating medium maintained at 500 degrees Fahrenheit is 6038 British thermal units. This is ⁇ all the energy that can beV extracted from a heat exchanger medium that will heat the two materials up to 500 degrees Fahrenheit.
  • the fiverpoundsrofl airU contains 580Britisli' thermal ⁇ units. 7.95 pounds: of:y steam resulfed" ⁇ containing 9550 ⁇ British thermalfunits a-nd2i05 pounds ofvwater with1020 B; t. u. fora totalof 1/l,.1'50 British thermal units'.-
  • the precipitated calcium: sulphate was periodically removedfrom the reactor.
  • the liquor leaving the reactor was ⁇ passed into the flash chamber. Froml this chamber the xed gases, i. e., nitrogen, carbon dioxide, 'and any excess air, were bled oifwith.steamatabout 1500 pounds per square inch gauge.
  • The. liquideluent from the flash chamber andthe condensate steam with the fixed gases had anV oxygen demand less thanl two percent of the oxygen demandof the raw waste sulte liquor.
  • the flow of feed liquor was adjusted so that the reactor was maintained about three-fourths full of liquid. ⁇
  • the amount of combustible material maintained in the reactor during the run was approximately forty times the amount of combustible material in the liquor fed into the reactor each hour. Air containing sucient oxygen to oxidize completely all ⁇ of the combustible material in the feed liquor was introduced simultaneously with the liquor. The oxidized products removed from the reaction zone balanced stoichiometrically the combustible materials in thefeed liquor. Over the course of several hours various runs demonstrated results as to reduction of oxygen demand ofthe feed liquor compared to the eiiuent comparable to that obtained in example one.
  • the explanatory data also shows that, by increasing the amount of combustible material within the reaction zone, the rate of oxygen consumption is increased independently of temperature and pressure.
  • the permissible Aconcentration of the oxidizable material in relation to the water inthe reaction zone is governed by the physical properties of this concentration especially as regards viscosity.
  • the viscosity must always be low enough to permit easy passage of gases and a smooth absorption of oxygen as well as a smooth segregation of the ash as it forms.
  • a suitable reactor was then devised for translating the results of the static experiment into a dynamic continuous process.
  • liquor which contained 4.44 pounds of solids wa-splaced in the reactor.
  • the reactor was maintained at 250 degrees centigrade and 800 pounds per square inch pressure.
  • the liquid level was observed through a sight glass and the level of the liquid was kept constant by the regulation of suitable heating and cooling devices.
  • Raw semi-chemical waste liquor was continuously introduced into thereactor with air containing7 the oxygen theoretically required to oxidize completely all of the'combustible materials' in the feed, so as to maintain Within the reactor an'amountv of combustible material having substantially the same ox ygen demand as the original reactor charge after equilibrium conditions are established.
  • reaction products were vented from the reactor and adequate energy was generated by the oxidation reaction to sustain the reaction temperature in the reactor, provide preheaty energy, and an excess of energy in utilizable form.
  • the reaction products were nitrogen, water vapor, carbon dioxide, and sodium sulfate, the latter removable as ash, or rendered soluble at other stages and removed as a solution.
  • the following chart illustrates material balanceony a per gallon feed basis for a prolonged run under thev conditions'abovedescribed Input-Pounds Liquor 8190 Solids-1.11 Water-7.79
  • waste effluent 1s suchthat1 it contains combustible matter susceptible of' being complete or substantially completely oxidizedto in-v nocuous endproducts underrelatively moderate temperature and pressure conditions.
  • the steps for capacity regulating which include: charging into a reaction zone a concentrated aqueous dispersion of combustible matter; introducing into said reaction zone a continuous feed of combustible materials dispersed in liquid water having a heat value concentration less than said reaction zone charge; introducing simultaneously into said reaction zone with said feed a continuous feed of an oxygen-containing gas in a stoichiometric amount to oxidize substantially completely all of said combustible materials in the feed; pressurizing said reaction zone to maintain at the temperature of the reaction at least some of the water therein in the liquid phase; varying the fuel value concentration of the charge in the reaction zone inversely proportional to the ratio of combustibles to water in the feed; regulating the introduction of feed and gas to said reaction zone at the rate of production of reaction products in the reaction zone to maintain the ratio of combustibles to water in the reaction zone; and, withdrawing reaction products, fixed gases and
  • the steps for regulating which include: providing in a reaction zone a charge of combustible materials dispersed in liquid water wherein the combustible materials are sutlicient in amount to supply Aat least the heat energy, upon substantially complete oxidation thereof, to maintain the temperature in the reaction zone above the autogenetic voxidation temperature at the rate at which a lower heat valve concentration dispersion is fed to the reaction zone; introducing into said zone an aqueous dispersion of combustible material having a heat value concentration less than said charge; introducing simultaneously alcontinuous feed of an oxygen-containing gas in amount stoichiometrically required to oxidize substantially completely lall of said combustible materials in the feed; initiating in said reaction zone a tiameless reaction proceeding at the rate at which said dispersion and gas are being fed to said zone; pressurizing the said zone to maintain at least some of the Water therein always remains in
  • the process for regulating the capacity of a continuous ameless autogenetic oxidation process for combustible materials dispersed in water in a reaction zone which includes: charging a reaction zone with a concentration of combustible material to water at least above the concentration of the feed; continuously passing a feed of combustible material dispersed in liquid water and an oxygen-containing gas into said reaction zone under superatmospheric pressure; withdrawing combustion products and water vapor at a rate which balances stoichiometrically the rate at which the combustible material and oxygen-containing gas are fed to said reaction zone to maintain the concentration of the charge of the reaction substantially constant in a ratio proportionally above the heat value concentration of the feed.
  • aqueous phase autogeneous oxidation of combustible material dispersed in water comprising: introducing into a reaction zone an aqueous dispersion of organic matter, having a heat content concentration substantially greater than that of an aqueous dispersion which is to be fed to the reaction zone, to establish a reaction mixture which will promote aqueous phase autogenous oxidation; introducing in a continuous manner into said reaction zone an aqueous feed having a heat content concentration substantially less than that first introduced into said reaction zone and in an amount equal to the rate of production of reaction products while simultaneously introducing with said feed an oxygen containing gas in an amount at least stoichiometrically suicient to oxidize all of said combustible matter in said feed; pressurizing the reaction zone to maintain at least a part of said aqueous dispersion inthe liquid phase at the autogenous oxidation temperature; and withdrawing reaction products, iixed gases and water vapor in an amount
  • reaction zone dispersion heat value concentration is varied substantially inversely proportional to the heat value concentration of said feed and substantially directly proportional to the volume of said feed.
  • the steps for regulating capacity which include: charging into a reaction zone a concentrated aqueous dispersion of combustible matter; introducing into said reaction zone a continuous feed of combustible materials dispersed in liquid Water having a heat value concentration less than said reaction zone with said -feed charge; introducing simultaneously into said reaction zone a continuous feed of an oxygen containing gas in a stoichiometric amount to oxidize substantially all of said combustible materials in the feed; pressurizing said reaction zone to maintain at the temperature of the reaction at least some of the water therein in the liquid phase; varying the fuel value concentration of the charge in the reaction zone inversely proportional to the ratio of com* bustibles to water in the feed; regulating the introduction of feed and gas to said reaction zone at the rate of production of reaction products in the reaction zone to maintain the ratio of combustibles to water in the reaction zone; withdrawing reaction products, iix

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FR1026068D FR1026068A (fr) 1953-12-14 1950-10-17 Procédé et installation pour la destruction par oxydation des matières organiques contenues dans des eaux-vannes telles que les liqueurs sulfitiques résiduaires et pour la production d'énergie-thermique
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Cited By (30)

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US2944396A (en) * 1955-02-09 1960-07-12 Sterling Drug Inc Process and apparatus for complete liquid-vapor phase oxidation and high enthalpy vapor production
US3079310A (en) * 1960-08-26 1963-02-26 James V Sheridan Electroplating zinc on aluminum
US3626874A (en) * 1968-10-22 1971-12-14 Action Concepts Technology Inc System for collecting and disposing of ordinary refuse by converting it into useful energy, without pollution
US3642620A (en) * 1969-10-14 1972-02-15 Texaco Inc Process for treating wastes from oxidation processes
US3738411A (en) * 1969-08-05 1973-06-12 Tatabanyai Szenbanyak Treatment of aluminate digester liquor
US3772181A (en) * 1968-11-29 1973-11-13 Texaco Inc Process for treating water-soluble organic wastes
US3901804A (en) * 1972-10-24 1975-08-26 Kanzaki Paper Mfg Co Ltd Method for processing sludge
US4013560A (en) * 1975-04-21 1977-03-22 Sterling Drug Inc. Energy production of wet oxidation systems
US4100730A (en) * 1975-06-04 1978-07-18 Sterling Drug, Inc. Regulation of a wet air oxidation unit for production of useful energy
US4229296A (en) * 1978-08-03 1980-10-21 Whirlpool Corporation Wet oxidation system employing phase separating reactor
US4234423A (en) * 1979-03-30 1980-11-18 The United States Of America As Represented By The United States Department Of Energy Energy recovery system
US4312761A (en) * 1980-05-28 1982-01-26 Zimpro-Aec Ltd. Treatment of clay slimes
US4330038A (en) * 1980-05-14 1982-05-18 Zimpro-Aec Ltd. Oil reclamation process
US4333529A (en) * 1979-08-31 1982-06-08 Wetcom Engineering Ltd. Oil recovery process
US4395339A (en) * 1982-04-01 1983-07-26 Sterling Drug Inc. Method of operating pure oxygen wet oxidation systems
US4524049A (en) * 1983-08-31 1985-06-18 Zimpro Inc. Process for concurrent steam generation and metal recovery
US5183577A (en) * 1992-01-06 1993-02-02 Zimpro Passavant Environmental Systems, Inc. Process for treatment of wastewater containing inorganic ammonium salts
WO1993004005A1 (fr) * 1991-08-22 1993-03-04 Titmas And Associates Incorporated Systeme de recuperation d'energie a partir de courants de procedes d'oxydation humide
US5268104A (en) * 1992-07-09 1993-12-07 Stone & Webster Engineering, Corp. Process for treating and regenerating spent caustic
US5551472A (en) * 1994-08-01 1996-09-03 Rpc Waste Management Services, Inc. Pressure reduction system and method
US5552039A (en) * 1994-07-13 1996-09-03 Rpc Waste Management Services, Inc. Turbulent flow cold-wall reactor
US5582715A (en) * 1992-04-16 1996-12-10 Rpc Waste Management Services, Inc. Supercritical oxidation apparatus for treating water with side injection ports
US5591415A (en) * 1994-01-27 1997-01-07 Rpc Waste Management Services, Inc. Reactor for supercritical water oxidation of waste
US5620606A (en) * 1994-08-01 1997-04-15 Rpc Waste Management Services, Inc. Method and apparatus for reacting oxidizable matter with particles
US5755974A (en) * 1994-08-01 1998-05-26 Rpc Waste Management Services, Inc. Method and apparatus for reacting oxidizable matter with a salt
US6001243A (en) * 1996-06-07 1999-12-14 Chematur Engineering Ab Heating and reaction system and method using recycle reactor
US6958122B1 (en) 1999-09-03 2005-10-25 Chematur Engineering Ab High pressure and high temperature reaction system
US20080073292A1 (en) * 2004-11-15 2008-03-27 Chematur Engineering Ab Reactor and Method for Supercritical Water Oxidation
US20080264873A1 (en) * 2004-11-15 2008-10-30 Anders Gidner Method and System for Supercritical Water Oxidation of a Stream Containing Oxidizable Material
US11187113B2 (en) * 2019-11-05 2021-11-30 Thomas R Bolles Method and apparatus for electrical power generation from natural gas with zero carbon emmision

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DE1136945B (de) * 1954-04-29 1962-09-20 William Jean Boulin Verfahren zur Reinigung von Kokereiabwasser
US2752243A (en) * 1954-06-24 1956-06-26 Sterling Drug Inc Ammonia-sulfur dioxide cooking acid regeneration
DE1252597B (de) * 1955-01-24 1967-10-19 Sterling Diug Inc New York NY (V St A) Verfahren zum Behandeln von dispergierte, oxydierbare, organische und gegebenenfalls anorganische Stoffe enthaltenden Abwassern und Vorrichtung zur Durchfuhrung des Verfahrens
DE1051210B (de) * 1955-03-11 1959-02-19 Koppers Gmbh Heinrich Abwasserreinigung durch Nassverbrennung der Verunreinigungen
DE1097415B (de) * 1956-01-24 1961-01-19 Sterling Drug Inc Verfahren zur sich selbst erhaltenden kontinuierlichen Oxydation waessriger Dispersionen brennbarer Stoffe
NL239038A (fr) * 1958-05-16

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US1268774A (en) * 1918-03-27 1918-06-04 Ingvar Soeraas Process of dissociating waste lye from the sulfite-cellulose manufacture.
US2213052A (en) * 1938-03-02 1940-08-27 Comb Eng Co Inc Method of and apparatus for the recovery of heat and chemicals from black liquor
US2258401A (en) * 1939-09-27 1941-10-07 Badenhausen John Phillips Treatment of waste liquids from pulp production and the like
US2665249A (en) * 1950-03-27 1954-01-05 Sterling Drug Inc Waste disposal

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US1268774A (en) * 1918-03-27 1918-06-04 Ingvar Soeraas Process of dissociating waste lye from the sulfite-cellulose manufacture.
US2213052A (en) * 1938-03-02 1940-08-27 Comb Eng Co Inc Method of and apparatus for the recovery of heat and chemicals from black liquor
US2258401A (en) * 1939-09-27 1941-10-07 Badenhausen John Phillips Treatment of waste liquids from pulp production and the like
US2665249A (en) * 1950-03-27 1954-01-05 Sterling Drug Inc Waste disposal

Cited By (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2944396A (en) * 1955-02-09 1960-07-12 Sterling Drug Inc Process and apparatus for complete liquid-vapor phase oxidation and high enthalpy vapor production
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