DK150785B - Apparatus for the treatment of substances in a liquid phase with a hot gas - Google Patents

Apparatus for the treatment of substances in a liquid phase with a hot gas Download PDF

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Publication number
DK150785B
DK150785B DK302179AA DK302179A DK150785B DK 150785 B DK150785 B DK 150785B DK 302179A A DK302179A A DK 302179AA DK 302179 A DK302179 A DK 302179A DK 150785 B DK150785 B DK 150785B
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combustion chamber
liquid phase
constriction
treatment
substances
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DK302179AA
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Danish (da)
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DK150785C (en
DK302179A (en
Inventor
Francois Prudhon
Augustin Scicluna
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Rhone Poulenc Ind
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00119—Heat exchange inside a feeding nozzle or nozzle reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00162—Controlling or regulating processes controlling the pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00164—Controlling or regulating processes controlling the flow
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Nozzles (AREA)
  • General Preparation And Processing Of Foods (AREA)

Description

150785150785

Opfindelsen omhandler et apparat til behandling af stoffer i en flydende fase med en varm gas og omfattende konstruktionsdele af den i krav l's indledning angivne art.The invention relates to an apparatus for treating substances in a liquid phase with a hot gas and comprising structural parts of the kind specified in the preamble of claim 1.

Fra tysk fremlæggelsesskrift nr. 2 528 559 kendes et 5 apparat til forbrænding af et flydende brændstof, der indsprøjtes i et af en perforeret cylinderflade afgrænset rum, mens luften til forbrændingen indføres fra en skruelinieformet strøm omkring den perforerede cylinderflade, og fra norsk fremlæggelsesskrift nr.German Patent Specification No. 2 528 559 discloses an apparatus for combustion of a liquid fuel injected into a space defined by a perforated cylinder surface, while the air for combustion is introduced from a helical stream around the perforated cylinder surface and from Norwegian Patent Specification no.

10 145 296 er det kendt via et "hoved" at tvinge en sådan skruelinieformet luftstrøm gennem en åbning med et mindre tværsnitsareal til en større behandlingsbeholder og at indføre en væske, der ønskes varmebehandlet, aksialt ved denne åbning, idet luftstrømmen har en meget stør-15 re bevægelsesmængde end væskestrømmen og medriver væsken i dette "hoved".It is known via a "head" to force such helical air flow through an aperture with a smaller cross-sectional area to a larger treatment vessel and to introduce a fluid which is desired to be heat treated axially at this aperture, the air flow having a very high flow rate. 15 more than the amount of movement and entrails the fluid in this "head".

Det har i praksis vist sig, at opvarmningen af dette "hoved" indvirker skadeligt på symmetrien af den hvirvel-brøndsagtige strømning, hvilket nedsætter apparatets 20 tilsigtede ydelse.In practice, it has been found that the heating of this "head" adversely affects the symmetry of the vortex-like flow, which decreases the intended performance of the apparatus 20.

Opfindelsen har til formål at afhjælpe denne ulempe ved at undvære det pågældende "hoved" og anvende de varme generatorgasser til en direkte dannelse af hvirvelbrønden til spredning af væskepartiklerne.The invention has the object of alleviating this disadvantage by avoiding the "head" in question and using the hot generator gases for a direct formation of the vortex well to disperse the liquid particles.

25 Forsøg har overraskende vist, at dette kan lade sig gøre, selv om der ud for indsnævringen opstår meget store temperaturgradienter, af størrelsesordenen op til flere hundrede °C pr. cm.25 Experiments have surprisingly shown that this can be done, although very large temperature gradients occur, of the order of up to several hundred ° C per annum. cm.

150785 2150785 2

Apparatet ifølge opfindelsen er ejendommeligt ved den i krav l's kendetegnende del angivne konstruktion.The apparatus according to the invention is characterized by the construction according to the characterizing part of claim 1.

Den indvendige skillevæg er fortrinsvis aftagelig og perforeret med cirkulære huller langs en strækning, der er 5 en funktion af varmeafgivelsen og af gastemperaturen. I det mindste ved den øvre, lukkede ende af apparatet skal forholdet imellem huldiameteren og vægtykkelsen overstige 5, og der bør være mindst seks huller fordelt langs mindst én cirkel, men fortrinsvis langs flere cirkler 10 på vægfladen. De fleste huller anbringes på skillevæggens øvre del for at fremme blandingen af de stoffer, der skal bringes i berøring med hinanden, og for at kunne forvarme en del af disse stoffer uden at beskadige inder-væggene som følge af den udviklede reaktionsvarme. Den 15 samlede overflade af hullerne på skillevæggens nedre del kan være meget lille, eksempelvis mellem 0,1 og 0,01 af hullernes samlede overflade.The inner partition is preferably removable and perforated with circular holes along a stretch which is a function of the heat release and of the gas temperature. At least at the upper closed end of the apparatus, the ratio of hole diameter to wall thickness should exceed 5, and there should be at least six holes distributed along at least one circle, but preferably along several circles 10 on the wall surface. Most holes are placed on the upper part of the partition to promote mixing of the substances to be contacted and to preheat some of these substances without damaging the inner walls as a result of the heat of reaction developed. The total surface of the holes on the lower part of the partition can be very small, for example between 0.1 and 0.01 of the total surface of the holes.

Betegnes den indvendige middeldiameter af den ydre kappe med og diameteren af den perforerede skil- 20 levæg med Do, er ^1 “ D2 fortrinsvis beliggende ^ 2 imellem 1 og 10 cm alt efter mængden af den skrue-linieformede strøm. Diameteren D2 bestemmes som funktion af den samlede varmefrigørelse fra reaktionen og ligger fortrinsvis imellem 0,4 og 0,5 Æ mm, hvor 25 k er det antal kilokalorier, som brændstoffet afgiver pr. time ved forbrændingen, eller i almindelighed den fremkaldte reaktion. D2 bør ikke være under 500 mm, når der i den retliniede strøm indføres et viskost reagerende middel, eksempelvis svær brænd-30 selsolie, der skal dispergeres fint og homogent.If the inner mean diameter of the outer sheath is denoted by and the diameter of the perforated partition wall with Do, ^1 1 D2 is preferably located 22 between 1 and 10 cm depending on the amount of helical stream. The diameter D2 is determined as a function of the total heat release from the reaction and is preferably between 0.4 and 0.5 µm, where 25 k is the number of kilocalories that the fuel emits per day. hour of combustion, or generally the evoked reaction. D2 should not be less than 500 mm when introducing into the rectilinear stream a viscous reactant, for example heavy fuel oil, which should be dispersed finely and homogeneously.

Bevægelsesmængden i den hvirvelbrøndsformede strøm skal være stor i forhold til væskernes, mindst 100 og fortrinsvis 1.000-10.000 gange større. Væskernes hastighed 150785' 3 nedsættes i øvrigt til det for deres kontinuerlige strømning minimalt krævede, medens gassernes hastighed kan forblive temmelig lille for ikke at kræve kraftige tryk.The amount of movement in the vortex-well flow must be large relative to that of the fluids, at least 100 and preferably 1,000-10,000 times greater. The speed of the liquids is further reduced to the minimum required for their continuous flow, while the velocity of the gases may remain rather low so as not to require high pressure.

5 Det hvirvelomstrømmende stof er i almindelighed en gas, som eventuelt medfører opslæmmede faststoffer eller væsker, der skal bringes i berøring med de ak-sialt indførte stoffer. Et tryk på 200-500 g/cm^ over det i åpparatets bageste del herskende tryk er 10 tilstrækkeligt til at sikre en god drift af apparatet.The eddy-flowing substance is generally a gas which optionally causes suspended solids or liquids to be brought into contact with the axially introduced substances. A pressure of 200-500 g / cm 2 above the pressure prevailing in the rear of the apparatus is sufficient to ensure good operation of the apparatus.

Den af strømmen fremkaldte hvirvelbevægelse fremkalder et let undertryk i den aksiale del, så at der kan opstå en væskestrømning i det indvendige rør uden at skulle udøve et tryk på denne væske.The eddy movement induced by the flow produces a slight underpressure in the axial portion so that a fluid flow can occur in the inner tube without having to exert pressure on this fluid.

15 Opfindelsen forklares nærmere nedenfor i forbindelse med tegningen, hvor: fig. 1 viser et apparat ifølge opfindels.en til almindelig behandling af en væske med en varm gas, fig. 2 viser apparatet med et ved udløbet fra behand-20 lingszonen anbragt efterbehandlingsapparat, især til støvudskilning, og fig. 3 viser apparatet med et tilsluttet afkølingsapparat .The invention is explained in more detail below in connection with the drawing, in which: 1 shows an apparatus according to the invention for the ordinary treatment of a liquid with a hot gas; FIG. 2 shows the apparatus with a finishing apparatus, located at the outlet of the treatment zone, in particular for dust removal, and FIG. 3 shows the apparatus with a connected cooling apparatus.

Som vist på fig. 1 omfatter apparatet ifølge opfin-25 delsen et forbrændingskammer 1 og et behandlingskammer 2.As shown in FIG. 1, the apparatus according to the invention comprises a combustion chamber 1 and a treatment chamber 2.

Forbrændingskammeret 1 omfatter en kappe 3, som ved sit øverste parti er aflukket med en dækplade 4, i hvilken der er udsparet en åbning til anbringelse af 4 150785 et forstøvningsorgan 5.The combustion chamber 1 comprises a sheath 3, which at its upper part is closed with a cover plate 4, in which an aperture for placing a spraying member 4 is recessed.

Forbrændingskammeret 1 omfatter et ringformet rum 6, som indadtil afgrænses af en cylinder 7, som er perforeret i den øvre del.The combustion chamber 1 comprises an annular space 6 which is delimited inwardly by a cylinder 7 perforated in the upper part.

5 En gas indføres tangentialt igennem et rør 8, der udmunder i det ringformede rum 6.5 A gas is introduced tangentially through a tube 8 which opens into the annular space 6.

Kappen 3 udløber i et konisk konvergerende område 9 med en indsnævring 10, i hvilket der i kammeret l's symmetriakse udmunder et bøjet rør 11 i det væsentlige 10 i højde med indsnævringen.The sheath 3 terminates in a conical converging region 9 with a constriction 10, in which, in the axis of symmetry of the chamber 1, a curved tube 11 is substantially 10 at the level of the constriction.

Behandlingskammeret 2 består af en dobbeltkegle, hvis forparti divergerer i forlængelse af indsnævringen 10.The treatment chamber 2 consists of a double cone whose front portion diverges in extension of the constriction 10.

På fig. 2 er der ved udløbet fra apparatets dobbeltkegle 2 anbragt et støvudskilningsapparat 12, der 15 omfatter en kappe 13, i hvilken der er anbragt en opfangningskegle 14 lige under dobbeltkeglen 2 og eventuelt også en væsketilgangsledning 15. Keglen 13 er selv forlænget med en cylinder 16, som muliggør en bevarelse af omdrejningsbevægelsen, og som 20 fører stofferne til en centrifugalseparator 17.In FIG. 2, at the outlet of the double cone 2 of the apparatus, a dust removal apparatus 12 is provided, which comprises a sheath 13 in which a trapping cone 14 is placed just below the double cone 2 and optionally also a liquid supply line 15. The cone 13 is itself extended by a cylinder 16, which permits a retention of the rotational motion and which leads the substances to a centrifugal separator 17.

De faste stoffer udløber ved 18 og gassen ved 19.The solids expire at 18 and the gas at 19.

På fig. 3 er der ved udløbet fra apparatets dobbeltkegle 2 anbragt et afkølingsapparat med et hoved 20, omfattende en perforeret væg 21, et tangentialrør 22, • . 25 et bøjet rør 23 og en cyklon 24.In FIG. 3, a cooling apparatus with a head 20, comprising a perforated wall 21, a tangential tube 22, is arranged at the outlet of the double cone 2 of the apparatus. 25 a bent tube 23 and a cyclone 24.

Behandlingskammeret 2 behøver ikke at være udført som en dobbeltkegle, men kan frembyde et cylindrisk midterparti .The treatment chamber 2 need not be designed as a double cone, but may provide a central cylindrical portion.

5 150785"5 150785 "

EKSEMPELEXAMPLE

Med det på fig. 2 viste apparat behandledes spildevand med et vægtindhold på 20% NaCl, 3-4% Na£S0^ og ca. 5% organiske stoffer omfattende polysulfider.With the FIG. 2, wastewater having a weight content of 20% NaCl, 3-4% Na₂SO ^ and approx. 5% organic matter comprising polysulfides.

5 Den samlede højde af forbrændingskammeret 1 var 193 mm, hvoraf de 43 mm for det konisk konvergerende område 9. Diametrene af kappen 3 var 120 mm og af den perforerede væg 7 82 mm. Diameteren af indsnævringen 10 var 18 mm, den udvendige diameter af røret 11 ud for indsnæv-10 ringen 10 var 12 mm, hvilket er 2/3 i forhold til diameteren af indsnævringen 10, og den indvendige diameter af røret 11 var 4 mm. Topvinkelen af dobbeltkeglen 2 var 90°.5 The total height of the combustion chamber 1 was 193 mm, of which 43 mm for the conically converging area 9. The diameters of the sheath 3 were 120 mm and of the perforated wall 7 82 mm. The diameter of the narrowing 10 was 18 mm, the outside diameter of the tube 11 next to the narrowing ring 10 was 12 mm, which is 2/3 of the diameter of the narrowing 10, and the inside diameter of the tube 11 was 4 mm. The top angle of the double cone 2 was 90 °.

Luftgennemstrømningen til forbrændingskammeret 1 igennem 15 røret 8 var 60 Nm^/h og trykket 0,4 bar=4xlO^Pa. Det igennem forstøvningsorganet 5 indsprøjtede brændstof bestod af propan, hvis indsprøjtning reguleredes således, at der opnåedes en temperatur på ca. 1.000°C ud for indsnævringen 10, og en igennem røret 11 tilført 20 spiIdevandsmængde reguleredes til opretholdelse af en temperatur af størrelsesordenen 500°C ved udløbet fra dobbeltkeglen 2.The air flow to the combustion chamber 1 through the pipe 8 was 60 Nm ^ / h and the pressure 0.4 bar = 4x10 0 Pa. The fuel injected through the atomizer 5 consisted of propane, the injection of which was regulated so as to achieve a temperature of approx. 1,000 ° C off the constriction 10, and a quantity of wastewater supplied through the pipe 11 was adjusted to maintain a temperature of the order of 500 ° C at the outlet of the double cone 2.

Det faste stof rummede for 30 kg behandlet spildevand 3 kg NaCl og 3 kg Na2S04. Det bemærkedes særligt, at 25 afgangsgassen ikke indeholdt fingods, og at den i det væsentlige bestod af vanddamp med spor af S02-The solid contained 30 kg of treated wastewater 3 kg of NaCl and 3 kg of Na2 SO4. In particular, it was noted that the exhaust gas did not contain any fines and that it consisted essentially of water vapor with traces of SO

Claims (4)

150785 - Patentkrav :150785 - Patent Claims: 1. Apparat til behandling af stoffer i form af en flydende, halvflydende eller dejagtig fase ved hjælp af en varm gas, omfattende et forbrændingskammer (1) og 5 et behandlingskammer (2) med en mellemliggende indsnævring (10), hvilket forbrændingskammer (1) er omgivet af en kappe (3), der foroven er aflukket ved en dækplade (4) og omslutter et ringformet rum (6), der indadtil er afgrænset af en perforeret skillevæg (7), og som 10 står i forbindelse med mindst én tangential indløbskanal (8) for en gas, og omfattende en igennem dækpladen (4) indragende aksial indløbskanal (5) for et brændstof, kendetegnet ved, at kappen (3) udløber i et konisk konvergerende område (9), i hvilket der langs 15 forbrændingskammerets (1) rotationsakse og ud for indsnævringen (10) udmunder en indsprøjtningskanal (11) for den flydende fase, og at behandlingskammeret (2) er anbragt koaksialt med og under forbrændingskammeret (1).An apparatus for treating substances in the form of a liquid, semi-liquid or dough phase by means of a hot gas, comprising a combustion chamber (1) and a treatment chamber (2) with an intermediate constriction (10), which combustion chamber (1) is enclosed by a casing (3) closed at the top by a cover plate (4) and encloses an annular space (6), which is inwardly delimited by a perforated partition (7) and which 10 communicates with at least one tangential an inlet duct (8) for a gas, comprising an axial inlet duct (5) projecting for a fuel, characterized in that the sheath (3) extends into a conical converging region (9) in which along the combustion chamber (1) axis of rotation and next to the constriction (10), an injection channel (11) opens for the liquid phase and the treatment chamber (2) is arranged coaxially with and below the combustion chamber (1). 2. Apparat ifølge krav 1, kendetegnet ved, at den inderste skillevæg (7) består af et aftageligt element.Apparatus according to claim 1, characterized in that the inner partition (7) consists of a removable element. 3. Apparat ifølge krav 1-2, kendetegnet ved, at det ringformede mellemrum (6) er cylinderringfor- 2. met.Apparatus according to claims 1-2, characterized in that the annular space (6) is cylindrical. 4. Apparat ifølge krav 1-3, kendetegnet ved, at forholdet imellem yderdiameteren af røret (11) for tilførselen af den flydende fase, og diameteren af indsnævringen (10) er mindst 1/4, fortrinsvis 2/3.Apparatus according to claims 1-3, characterized in that the ratio between the outer diameter of the pipe (11) for the supply of the liquid phase and the diameter of the constriction (10) is at least 1/4, preferably 2/3.
DK302179A 1978-07-21 1979-07-18 Apparatus for the treatment of substances in a liquid phase with a hot gas DK150785C (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR7821658A FR2431321A1 (en) 1978-07-21 1978-07-21 PROCESS FOR THE TREATMENT OF SUBSTANCES HAVING DIFFERENT PHASES, SUCH AS TREATMENT OF SUBSTANCES IN LIQUID, SEMI-LIQUID, OR PASTE FORM, WITH ANOTHER NOTABLY GASEOUS PHASE
FR7821658 1978-07-21

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DK302179A DK302179A (en) 1980-01-22
DK150785B true DK150785B (en) 1987-06-22
DK150785C DK150785C (en) 1988-01-18

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EP (1) EP0007846B1 (en)
JP (1) JPS5520696A (en)
AR (1) AR225419A1 (en)
AT (1) ATE901T1 (en)
AU (1) AU530971B2 (en)
BR (1) BR7904641A (en)
CA (1) CA1132850A (en)
DE (1) DE2962620D1 (en)
DK (1) DK150785C (en)
ES (1) ES482686A1 (en)
FI (1) FI72709C (en)
FR (1) FR2431321A1 (en)
IE (1) IE49618B1 (en)
IN (1) IN152322B (en)
MA (1) MA18535A1 (en)
NO (1) NO152087C (en)
PT (1) PT69949A (en)
ZA (1) ZA793747B (en)

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FR2488525A1 (en) * 1980-08-14 1982-02-19 Rhone Poulenc Ind Mixing of two fluids present as different phases - esp. for heat or mass transfer between gas and liq.
FR2490619A1 (en) * 1980-09-24 1982-03-26 Rhone Poulenc Ind PROCESS FOR TREATING LIQUID MATERIAL CONDUCTING SOLID WASTE BY ACTION OF A FLUID PHASE AND AT LEAST ONE GAS PHASE
FR2501525A1 (en) * 1981-03-13 1982-09-17 Rhone Poulenc Spec Chim DEVICE FOR CONTACTING SUBSTANCES IN DIFFERENT PHASES, AT LEAST ONE GAS BEING
FR2508888A1 (en) * 1981-07-06 1983-01-07 Rhone Poulenc Chim Base NOVEL SODIUM ORTHOPHOSPHATE, PROCESS FOR OBTAINING SAME
FR2508818A1 (en) * 1981-07-06 1983-01-07 Rhone Poulenc Chim Base METHOD FOR THE HOMOGENEOUS THERMAL AND / OR CHEMICAL TREATMENT OF A FLUID, AND APPLICATION TO POLYPHOSPHATES
FR2508887A1 (en) * 1981-07-06 1983-01-07 Rhone Poulenc Chim Base NOVEL SODIUM TRIPOLYPHOSPHATE, PROCESS FOR OBTAINING SAME AND APPLICATIONS
FR2531059A1 (en) * 1982-07-27 1984-02-03 Rhone Poulenc Chim Base High hydration rate sodium tripolyphosphate
EP0101347B1 (en) * 1982-07-27 1986-09-24 Rhone-Poulenc Chimie De Base Sodium tripolyphosphate having a high hydration rate, and detergent composition containing it
US4499833A (en) * 1982-12-20 1985-02-19 Rockwell International Corporation Thermal conversion of wastes
US4579069A (en) * 1983-02-17 1986-04-01 Rockwell International Corporation Volume reduction of low-level radioactive wastes
FR2546077B1 (en) * 1983-05-20 1988-05-06 Rhone Poulenc Chim Base HIGH TEMPERATURE REACTION DEVICE
FR2551183B1 (en) * 1983-05-20 1988-05-13 Rhone Poulenc Chim Base OWN COMBUSTION PROCESS AND DEVICE APPLICABLE IN PARTICULAR TO THE BURNING OF HEAVY FUELS
GB2177618B (en) * 1985-07-13 1989-07-19 Adrian Philip Boyes Gas/liquid contacting
FR2587915B1 (en) * 1985-09-27 1987-11-27 Omya Sa DEVICE FOR CONTACTING FLUIDS IN THE FORM OF DIFFERENT PHASES
JPS62179984U (en) * 1986-05-02 1987-11-14
US4767543A (en) * 1986-11-13 1988-08-30 Universite De Sherbrooke Oxidation of wastewaters
JPH0540769Y2 (en) * 1987-11-16 1993-10-15
EP0545757A1 (en) * 1991-11-29 1993-06-09 Rhone-Poulenc Chimie Process for the preparation of perovskites on the basis of manganese or chromium and perovskites so obtained
FR2684659A1 (en) * 1991-12-06 1993-06-11 Rhone Poulenc Chimie Glass or glass-ceramic precursor and process for its preparation
FR2698156B1 (en) * 1992-11-16 1995-01-27 Rhone Poulenc Chimie Process for the thermal treatment of an effluent comprising polluting organic materials or an inorganic compound.
FR2718371B1 (en) * 1994-04-08 1996-05-03 Rhone Poulenc Chimie Reduction catalysts for nitrogen oxides based on spinels.
FR2720296B1 (en) 1994-05-27 1996-07-12 Rhone Poulenc Chimie Compounds based on alumina, cerium oxide and zirconium oxide with high reducibility, process for their preparation and their use in the preparation of catalysts.
FR2720295B1 (en) 1994-05-27 1996-07-12 Rhone Poulenc Chimie Dispersible compound based on a rare earth, colloidal suspension obtained from this compound, their methods of preparation and use in the manufacture of catalysts.
FR2826016B1 (en) 2001-06-13 2004-07-23 Rhodia Elect & Catalysis COMPOUND BASED ON AN ALKALINE EARTH, SULFUR AND ALUMINUM, GALLIUM OR INDIUM, METHOD FOR PREPARING SAME AND USE THEREOF AS LUMINOPHORE
FR2855169B1 (en) 2003-05-23 2006-06-16 Rhodia Elect & Catalysis PRECURSOR COMPOUNDS OF ALKALINO-EARTH OR RARE EARTH ALUMINATES, PROCESS FOR THEIR PREPARATION AND THEIR USE AS A LUMINOPHORE PRECURSOR, IN PARTICULAR
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CN109357270A (en) * 2018-11-21 2019-02-19 贵州智慧能源科技有限公司 A kind of device being capable of handling complex component sewage
WO2021111001A1 (en) 2019-12-06 2021-06-10 Solvay Sa Aluminates and red emitters in a greenhouse film for plant growth
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ATE901T1 (en) 1982-05-15
AU4867279A (en) 1980-01-24
ZA793747B (en) 1980-08-27
FR2431321B1 (en) 1981-03-20
NO152087B (en) 1985-04-22
PT69949A (en) 1979-08-01
CA1132850A (en) 1982-10-05
IN152322B (en) 1983-12-17
IE791379L (en) 1980-01-21
FI72709B (en) 1987-03-31
JPS6132045B2 (en) 1986-07-24
ES482686A1 (en) 1980-04-16
NO792392L (en) 1980-01-22
DK150785C (en) 1988-01-18
NO152087C (en) 1985-07-31
FI792279A (en) 1980-01-22
EP0007846A1 (en) 1980-02-06
JPS5520696A (en) 1980-02-14
FR2431321A1 (en) 1980-02-15
MA18535A1 (en) 1980-04-01
FI72709C (en) 1987-07-10
AR225419A1 (en) 1982-03-31
DE2962620D1 (en) 1982-06-09
IE49618B1 (en) 1985-11-13
AU530971B2 (en) 1983-08-04
DK302179A (en) 1980-01-22
BR7904641A (en) 1980-04-15
EP0007846B1 (en) 1982-04-28

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