EP0091948A1 - Procede de production de sulfures par ecoulement d'une couche en fusion - Google Patents

Procede de production de sulfures par ecoulement d'une couche en fusion

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Publication number
EP0091948A1
EP0091948A1 EP82903536A EP82903536A EP0091948A1 EP 0091948 A1 EP0091948 A1 EP 0091948A1 EP 82903536 A EP82903536 A EP 82903536A EP 82903536 A EP82903536 A EP 82903536A EP 0091948 A1 EP0091948 A1 EP 0091948A1
Authority
EP
European Patent Office
Prior art keywords
alkali metal
reaction zone
process according
melt
oxysulfur
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP82903536A
Other languages
German (de)
English (en)
Other versions
EP0091948A4 (fr
Inventor
Arthur L. Kohl
Leroy F. Grantham
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Combustion Engineering Inc
Original Assignee
Combustion Engineering Inc
Rockwell International Corp
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 Combustion Engineering Inc, Rockwell International Corp filed Critical Combustion Engineering Inc
Publication of EP0091948A1 publication Critical patent/EP0091948A1/fr
Publication of EP0091948A4 publication Critical patent/EP0091948A4/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/22—Alkali metal sulfides or polysulfides
    • C01B17/24—Preparation by reduction
    • C01B17/26—Preparation by reduction with carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • 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
    • D21C11/125—Decomposition of the pulp liquors in reducing atmosphere or in the absence of oxidants, i.e. gasification or pyrolysis

Definitions

  • the present invention relates to a process for the production of alkali metal sulfides by reduction of the corresponding oxysulfur compounds, that is, compounds containing alkali metal, oxygen and sulfur, such as alkali metal sulfites or sulfates, using a solid carbonaceous reducing agent.
  • thi invention relates to such a process in which there is forme a melt which is caused to flow in a layer along the periphe of a reaction zone into which the reactants are introduced.
  • Alkali metal sulfides as industrial chemicals have a wide variety of end uses. They are also used as intermediates in flue gas desulfurization processes in which sulfur values are recovered from gases produced in burning sulfur-containing fuels and in other industrial processes.
  • U.S. Pat. No. 1,212,702 describes a process for reducing sodium sulfate or sodium bisulfate to sodium sulfide in a shaft furnace in which a reducing atmosphere is maintained by feeding a controlled amount of air to burn large pieces of carbonaceous matter, such as coal or coke.
  • the sulfate or bisulfate salt is mixed with an excess of coal, charged into the reducing atmosphere of the furnace, . and the salt melted and reduced over the heated carbonaceous matter at a temperature of about 1000 C.
  • 3,867,251 discloses a process for producing alkali metal carbonates and alkali metal sulfides from evaporated alkaline cooking liquor obtained from pulp production which utilizes a horizontal combustion cyclone to produce turbulence within a reaction chamber.
  • the cooking liquor is pyrolyzed to alkali metal carbonate, carbon and hydrogen sulfide in a first zone, into which a hot oxygen- containing gas is introduced tangentially at a temperature of about 700°C.
  • a second zone into which hot flue gases are injected tangentially, alkali metal carbonate in the form of a smelt reacts with hydrogen sulfide to form alkali metal sulfide at a temperature of about 900°C.
  • combustion gases are oxidized by means of tangentially injected oxygen-containing gas at a temperature of about 1100° to 1200°C.
  • U.S. Pat. No. 4,198,385 discloses a two-stage process for the reduction of sodium sulfate accumulated in spinning baths during viscose fiber manufacture.
  • a reducing atmosphere is provided at a temperature greater than the melting point of sodium sulfide, so that molten sodium sulfide plus unreacted sodium sulfate collects in a melt at the bottom of a combustion chamber.
  • a separately applied reducing agent and inert exhaust gases are introduced into the melt to agitate the melt and to produce additional, sodium sulfide from unreacted sodium sulfate.
  • the sodium sulfide can then be reacted with zinc oxide to produce sodium hydroxide for use in the spinning baths.
  • the conversion of oxysulfur compounds to sulfides is particularly important in plants which are designed to remove sulfur oxides from the flue gases of power plants generating electricity by the combustion of fossil fuels.
  • sulfur oxide impurities are removed from a hot combustion gas by contacting the gas at a temperature of at least about 350 C. with a molten salt mixture containing alkali metal carbonates as the active absorbent.
  • the molten absorbent solution containing the absorbed sulfur values, principally as alkali metal sulfites, is treated with a reductant gas mixture containing hydrogen, carbon monoxide, or a mixture thereof, at a temperature of at least about 400°C.
  • the molten salt containing the alkali metal sulfides is treated with a gaseous mixture containing steam and carbon dioxide at a temperature below about 450°C. , to regenerate the alkali metal carbonates and convert the alkali metal sulfides to hydrogen sulfide gas which can be converted to sulfur or sulfuric acid.
  • the reduction step is accomplished in a large pool-type reactor held at about 1000°C.
  • the spent salt is fed into the reactor together with a solid carbonaceous reducing agent such as petroleum coke or coal.
  • Air is also fed into the reactor through feed nozzles located below the surface of the melt. The air serves primarily as a source of oxygen which reacts with a portion of the reducing agent exothermally to provide heat for the system.
  • This reaction generates typical combustion gases such as carbon monoxide, carbon dioxide and water vapor, which bubble through the molten salt pool together with the nitrogen from the air feed. Gases which are produced by the chemical reduction reaction join the combustion product gases, and the mixed gas stream leaves the reactor as product gas. Oxysulfur compounds in the spent salt feed are largely reduced to sulfide by the carbon present in the pool. Molten salt containing the sodium sulfide product, sodium carbonate from the original feed plus small amounts of unreacted carbon and oxysulfur compounds is withdrawn from the molten pool by an overflow system. Gases leave the vessel via a discharge port near the top.
  • a second problem with this kind of reactor design is the difficulty in maintaining constant melt-discharge rate. For example: A slight increase in air rate will cause the melt level to increase because of the increased number of bubbles within it. This causes a great increase in the instantaneous melt overflow rate which, in turn, can represent a safety as well as operational problem for the melt quench step which follows.
  • Another object of this invention is to provide a reduction process utilizing molten salts which does not require the molten salt pools " of the prior art.
  • Yet another object of this invention is to provide su a process which can be conducted in a relatively simple apparatus.
  • an alkali metal oxysulfur compound is converted into the corresponding alkali metal sulfide by a process which comprises introducing an alkali metal oxysulfur compound and a solid carbonaceous reducing agent into a reaction zone; subjecting the oxysulfur compound and reducing agent to centrifugal force; heating the reaction zone to melt the oxysulfur compound and to cause the oxysulfur compound and reducing agent to react to produce alkali metal sulfide; flowing a melt containing the alkali metal sulfide thereby produced, unreacted oxysulfur compoun and unreacted reducing agent through the reaction zone and along the periphery thereof, to cause the unreacted oxysulfur compound and the unreacted reducing agent to reac to produce additional alkali metal sulfide; and recovering.
  • the centrifugal force to which the oxysulfur compound and reducing agent are subjected is produced by tangential injection of at least one of the oxysulfur compound and the solid carbonaceous reducing agent entrained in a gaseous stream.
  • FIG. 1 is a schematic diagram, partly in cross section of one embodiment of apparatus which can be used in carryin out the process of the present invention, wherein product
  • OMPI gas and product melt are discharged together through a single nozzle directly into a quench tank containing an aqueous solution.
  • FIG. 2 is a schematic diagram, partly in cross section, of another embodiment of apparatus suitable for use in this invention, wherein a major portion of the product gas is withdrawn by way of a centrally located discharge port near the top of the reactor, and product melt is discharged into a quench tank through a nozzle near the bottom of the reactor.
  • FIG. 3 is a schematic diagram, partly in cross section, of a third embodiment of apparatus which can be used in the present invention, wherein product melt and product gas are discharged into a cooling zone designed to solidify the product melt into a granular product.
  • FIG. 4 is a section taken along lines 4-4 of FIG. 3. Description of the Preferred Embodiments
  • the present invention provides a continuous process for the reduction of oxysulfur compounds which uses a simple reactor of compact design with a low-cost solid carbonaceous material such as coal or petroleum coke as the reducing agent.
  • Equations 1, 2, 3, and 4 illustrate possible routes to the reduction of some of the -most common oxysulfur compounds encountered in practicing the process of the present invention.
  • Equations 5 and 6 depict reduction by the hydrogen combined with carbon in th solid carbonaceous reducing agent.
  • Equation 7 illustrates the disproportionation reaction which results in the formation of additional alkali metal sulfate when the alkal metal sulfite in the reactant stream disproportionates rather than being reduced in accordance with one of Equations 3, 4, or 6 shown above.
  • the alkali metal sulfate whic forms can be reduced to alkali metal sulfide in accordance with Equation 1, 2, or 5.
  • a simple reactor in which the reactions illustrated above are caused to take place at least partly in a melt layer which flows down the inside walls of the reactor.
  • the reactor is heated and the mixture of heated reactants subjected to centrifugal force to cause the formation of a melt layer upon the walls of the reactor.
  • the heated reactants are subjected to centrifugal force by injecting a least a part of the reactants tangentially into a reactor o circular cross section. In this manner, the heated oxysulfur compounds are melted and follow a spiral path downwards in the reactor and under the influence of centrifugal force become deposited along the walls of the reactor together with unreacted particles of carbonaceous reducing agent.
  • the resulting melt layer moves downward along the walls during the time that the reaction between the oxysulfur compound and the solid carbonaceous reducing agent is proceeding.
  • the flowing melt layer exits the reactor at the bottom thereof and is cooled by contact with cool gases or by being introduced into an aqueous quench solution.
  • the reduced oxysulfur compounds are soluble in the aqueous quench solution and may be recovered therefrom.
  • the aqueous solution containing the quenched melt may be removed and further processed to recover the desired alkali metal sulfides from the solution.
  • the recovered sulfides may be further processed to regenerate alkali metal carbonates or bicarbonates which
  • the temperatures utilized in the reactor may be lower than those wherein the salt mixture contains merely sulfates or sulfites.
  • the product gases may be removed from the reactor and likewise further processed in order to recover valuable byproducts.
  • the carbon monoxide content may be burned to provide heat and form additional carbon dioxid and the carbon dioxide content may be used to drive hydroge sulfide from sulfide solutions in accordance with the following reactions:
  • Hydrogen sulfide may be separated and converted to sulfur i a Claus plant or utilized in the manufacture of sulf ric acid.
  • the product gases may be removed from the top of the reactor or they may be removed from the bottom of the reactor along with the melt, as desired.
  • Heat for the reduction reaction may be produced by means of a suitable burner incorporated with the reactor or may be produced by oxidation of a portion of the carbonaceous reducing agent.
  • the reduction reaction is suitably carried out at an elevated melt temperature, usually in the range of about 900° to 1400°C, and preferably in the range of about 950° to 1150°C.
  • an elevated melt temperature usually in the range of about 900° to 1400°C, and preferably in the range of about 950° to 1150°C.
  • One of the principal advantages of the present invention is that external heating of the reactor is not required. Rather, heating to produce the required melt temperature is accomplished in situ by the combustion of a* fuel by a moving stream of an oxidizing gas.
  • the oxidizing gas serves two purposes, namely, causing combustion of the fuel used to heat the reaction zone and propelling particles of reactants in a spiralling path within the reaction zone in a way such that the particles melt and the resulting mel
  • OMPI flows in a layer at the outer periphery of the reaction zone.
  • the thus-produced flowing melt layer enables the reactants to be in contact for a longer period of time than if the reactants reacted only directly in the stream of oxidizing gas without forming such a flowing melt layer.
  • the process of the instant invention can be used to convert a wide variety of oxysulfur compounds to the corresponding alkali metal sulfides.
  • Some of the more common oxysulfur compounds include lithium sulfite, sodium sulfite, potassium sulfite, lithium sulfate, sodium sulfate, and potassium sulfate as well as other alkali metal sulfite and sulfates.
  • Bisulfates, bisulfites, thiosulfates, and sulfonates can also be converted to sulfides in accordance with the process of this invention.
  • any of a wide number of solid carbonaceous materials are satisfactory. Coal or petroleum coke is preferred. Other forms of carbonaceous materials are also suitable. For example, asphalt, peat, lignite, or wood may be used.
  • alkali metal halides for example, sodium chloride or alkali metal carbonates or bicarbonates, such as sodium carbonate and sodium bicarbonate have been found particularly satisfactory. They may be used in an amount of up to about 50% of the oxysulfur compound.
  • the carrier gas used to introduce reactants into the reactor can be an oxidizing gas, such as oxygen or air, or it may be an inert gas such as nitrogen or flue gas. It is used, in general, in an amount sufficient to entrain the reactants, principally the alkali metal oxysulfur compound and finely divided solid carbonaceous reducing agent. If an oxidizing gas is-used, it will function both as an oxidizer and as a carrier and must be added in sufficient quantity to provide both functions. An oxidizer is desirable in order to oxidize a portion of the carbonaceous material which is used as the reducing agent in the reaction. Oxidation of the carbonaceous material results in the release of a large amount of heat, since such a reaction is highly exothermic.
  • an oxidizing gas such as oxygen or air
  • an inert gas such as nitrogen or flue gas
  • Heat is required not only for melting the oxysulfur compound and for keeping the product sulfides in the molten state, but also for the carrying out of the endothermic reduction reactions which are carried out in the reactor.
  • the use of such an auxiliary burner is not deemed essential, since adequate heat can be furnished by oxidation of a part of the carbonaceous reducing agent in the reactor.
  • a separate burner to provide part of the heat required and to use an oxidizing gas, such as air or oxygen, as the carrier gas to furnish part of the heat by oxidation of a portion of the carbonaceous material entrained in the oxidizing gas.
  • an oxidizing gas such as air or oxygen
  • the starting materials utilized in this invention containing the oxysulfur compound and which may also contain, for example, alkali metal carbonate and other alkali metal salts as well, can be obtained from various industrial processes.
  • a convenient source of oxysulfur compounds can be the spent absorbent from processes used to desulfurize flue gases from plants burning fossil fuels, spent sulfite "black liquor” from paper mills or spent "seed” from magnetohydrodynamic (MHD) power plants.
  • the principal oxysulfur compound produced is potassium sulfate which is generated when potassium carbonate, added to high temperature combustion
  • OMPI gases to increase electrical conductivity also absorbs sulfur compounds in the gases.
  • the oxysulfur compoun can be derived from a number of process streams.
  • ACP aqueous carbonate process
  • reducing agent in each droplet of sodium carbonate solution while it is absorbing sulfur dioxide and being dried also acts to inhibit the oxidation of sulfite t sulfate.
  • Adding the reducing agent prior to drying permits use of an aqueous slurry of reducing agent.
  • sewage sludge or a coal slurry may be used.
  • the mixture of sodium carbonate, reducing agent and water is then sprayed into a hot sulfur dioxide-containing gas in the usual manner, whereby efficient contact between liquid droplets and gas is obtained and a dry powder containing both sodium sulfite and reducing agent is obtained as the product of th sulfur dioxide absorption — drying step in the ACP process. This technique obviates the need for mixing reactants in th reactor.
  • the amounts of solid carbonaceous material, burner fuel, and oxidizing gas required to produce a given amount of alkali metal sulfide will depend upon the nature of the oxysulfur compound feed, the percent conversion desired, the reactor design, and other factors. For example, if the carbonaceous material is carbon and the oxysulfur compound is pure sodium sulfate, at least 2 moles of carbon are required per mole of feed salt for the reduction alone. In addition, fuel and oxidizing gas are required in sufficient amounts that their combustion will provide all of the heat necessary to melt the feed salt, provide the heat for endothermic reduction reactions, raise the temperature of all products to their discharge temperatures, and provide for any heat losses from the system.
  • All or a portion of the required fuel may be in the form of the solid carbonaceous material.
  • the total amount of reactive carbon and hydrogen in both the solid carbonaceous reducing agent and the combusion fuel must be in excess of the stoichiometric amount required to convert all of the oxygen in the oxysulfur compounds and the oxidizing gas to carbon dioxide and water.
  • the reactants can be introduced into the reactor in a number of different ways depending upon the result sought and the type of starting materials which are used.
  • the mos desirable configurations are those in which the combustion mixture and the mixture of oxysulfur compounds, reducing agent, and carrier gas are introduced through separate ports.
  • This combination of gas streams results in producing the desired spiral path for the reactants and also realizing optimal heating conditions for the reactant stream.
  • air is used as both the carrier gas and the oxidant
  • coal is used as the carbonaceous material functioning as both the reducing agent and the oxidizable fuel
  • a mixture of sodium sulfite, sodium sulfate and sodium carbonate is the salt mixture.
  • coal and approximately one-half of the air is introduced axially to the reactor through a burner which imparts a swirling flow to the combustion products, while a mixture of salts, coal and the remainder of the air is introduced tangentially.
  • OMPI are propelled through the reactor in a spiral path, the desired melt formation takes place in the traversal of the spiral path through the reactor and the melt is deposited upon the wall of the reactor and flows down the wall as the reaction proceeds.
  • the oxysulfur compounds fed to the reactor are reduced to the corresponding sulfides.
  • the feed consists of sodium sulfite and sodium sulfate
  • sodium sulfide is produced. Since the reaction takes place in a flowing layer of melt, the product sulfide is recovered as a melt.
  • Melt residence time within the reactor may vary within a wide range depending upon the velocity of the reactant stream within the reactor, the temperature and pressure of the reactor and the length of the reaction zone within the reactor. In general, melt residence times less than about 2 minutes and preferably about 5 to 60 seconds are used. The residence time is adjusted to be long enough to insure that at least about 80% of the oxysulfur compound introduced into the reactor is reduced to sulfide.
  • the product melt exiting the reactor must be cooled in order to enable recovery of the sulfide for its use in further processing.
  • the melt flows into a water bath or is contacted by a spray of liquid water.
  • an aqueous solution containing previously dissolved melt or other process salts may be used. Provision is made for the removal of the gaseous products of the reaction as well as the products present in the melt.
  • the aqueous solution containing the quenched melt may be drawn off from the quench tank and subjected to further processing including recovering relatively pure alkali metal sulfide from the solution, in accordance with known procedures.
  • a gas-contacting device such as a prilling tower is utilized.
  • the melt containing the sulfide product is blown through a discharge nozzle at the bottom of the reactor by the gases formed during the reactions taking place within the reactor and is formed into small droplets. These droplets harden into fin shot-like beads or prills as a result of contacting relatively cool gas in the prilling tower. Gas is continuously removed from the prilling tower, cooled and reinjected to provide the means for cooling and solidifying the prills.
  • the prills containing alkali metal sulfide, fall to the bottom of the prilling tower and are collected in a bed either in the tower or in a separate vessel as desired. Gas containing carbon dioxide and water vapor is passed through the bed at a temperature below the melting point of the salts and preferably in the range of about 250 to 650°C.
  • the alkali metal sulfide is thereby converted to al ali metal bicarbonate or carbonate in accordance with Equations 8 or
  • the gas produced in the reduction is used as the source of carbon dioxide for these reactions.
  • This gas contains an adequate supply of carbon dioxide and can be enriched in water vapor, if necessary, by the injection of liquid water or steam. Because of their special shape, the prills form porous high surface area packed bed which is permeable to the flow of gas and does not hang up or plug in the contact zone.
  • the use of the prilling tower for recovering solid alkali metal sulfide from the reduction reactor can also be taken advantage of in MHD feed regeneration and the regenerated prills recycled directly to the MHD combustor. Ash compounds which were in the original seed or were added with coal in the reducer will be decomposed by the high temperature in the MHD combustor and redistributed downstream of the MHD channel so that only a small portion reappears in the spent seed. In this way the ash in the seed can be recycled to extinction with all of this eventually leaving via the main discharge point for coal as which passes throu ⁇ h the channel.
  • OMPI When used for the regeneration of spent salt for flue gas desulfurization, it is desirable to remove ash and produce the regenerated carbonate in the form of an aqueous solution. To accomplish this, the prills are dissolved in water which is filtered or otherwise separated to produce a solution of sodium carbonate and an insoluble ash cake.
  • the prilling tower recovery process described above is given as one example of a gas/particle contact process.
  • the products of the process of this invention include not only the melt referred to above, which is a source of the alkali metal sulfide, but also gases which are produced in the various reactions occurring in the reactor. These gases include carbon monoxide, carbon dioxide and water vapor.
  • gases include carbon monoxide, carbon dioxide and water vapor.
  • the production of a gaseous product having a C0 2 :CO ratio of at least about 1:1 is desirable. With this ratio being realized, the carbonaceous material is substantially used up in the reactor.
  • the appreciable quantity of carbon dioxide present in the gaseous product can be used for carbonate regeneration if desired.
  • a reactor 10 is a vessel of circular cross section lined with a corrosio resistant refractory 12, such as fusion cast alumina blocks within a metal containment 14.
  • Reactor 10 has a tangential entry nozzle 16 located near the top of the reactor and a discharge nozzle 18 located at the bottom of the reactor.
  • mixture of salts containing oxysulfur compounds and pulverized solid carbonaceous reducing agent, such as coal, is introduced into reactor 10 through tangential entry nozzle 16 via a line 20.
  • Air is supplied via a line 22 to entrain the salt-coal mixture.
  • the top of reactor 10 is provided with a burner 24, which includes a tangential entr nozzle 26 and an axial entry nozzle 28.
  • Air is supplied through tangential entry nozzle 26 via a line 30, and combustion coal is supplied to axial entry nozzle 28 via a line 32.
  • a flame 34 is shown* exiting burner 24 and occupying the top part of reactor 10.
  • a spiral path 36 represents the course followed by the mixture of salt and reductant coal, which is introduced together with a carrier air stream through tangential entry nozzle 16.
  • a melt 38 shown along an inside wall 40 of reactor 10, is formed as molten salt particles and associated particles of reducing agent are thrown to wall 40 by the action of centrifugal force. Melt 38 proceeds downwardly in a moving layer along the inside wall 40 of reactor 10 and exits reactor 10 through discharge nozzle 18, together with product gases.
  • the mixture of melt and product gases enters a quench tank 42, containing an aqueous quench solution 44.
  • Quench tank 42 is equipped with an exit nozzle 46, through which the off-gases are removed via a line 48.
  • the product salts can be recovered from quench solution 44 and further processed as desired.
  • FIG. 2 differs from that of FIG. 1 primarily in the manner of removing product gas.
  • a reactor 100 is of circular cross section and
  • Quench tank 114 is equipped with an aqueous solution feed nozzle 122, through which the aqueous quench solution is fed to quench tank 114 via a line 124; a quenched melt discharge nozzle 126, through which aqueous solution containing the quenched melt is discharged via a line 128; and gas discharge nozzle 130, through which product gases from quench tank 114 are discharged via a line 132.
  • reactor 200 is a circular cross-section reactor lined with a corrosion- resistant refractory 202, such as fusion-cast alumina blocks, surrounded by a thermally insulating castable refractory 204 within a metal containment 206.
  • Reactor 200 is equipped with two tangential feed nozzles 208 in the upper portion of reactor 200 and a discharge nozzle 210 at the bottom thereof.
  • a feed hopper 212 is adapted for controlled feeding of a feed mixture 214 of salts containin oxysulfur compounds and pulverized solid carbonaceous reducing agent into a line 216 through which it is conveyed to at least one of the feed nozzles 208 by a carrier gas such as air.
  • the carrier gas enters via a feed line 218 an a blower 220.
  • a separate burner 222 is shown with its own fuel line 224 and air supply line 226.
  • Discharge nozzle 21 is designed to increase the velocity of the discharge gas sufficiently to cause it to produce breakup of the melt formed in reactor 200.
  • Melt flows downwardly along an inside wall 228 of reactor 200 and with product gas is discharged through nozzle 210 into a melt solidification chamber 230.
  • Gas is continuously removed from this chamber via a line 232, cooled in a heat exchanger 234 by means of heat recovery fluid and returned to chamber 230 via a line 236.
  • Gas circulation is forced by a blower 238 and an amount of product gas equal to the net amount of gas produced in the reactor is continuously removed from the system via a line 240.
  • Cooling in chamber 230 is accomplished by simple contact of falling droplets with a rising stream of cool gas.
  • Alternative cooling techniques such as fluidized beds or rotary granulators may be employe within the scope of this invention.
  • EXAMPLE 1 A unit was constructed having the general configuratio of the reactor and fuel system of FIG. 3.
  • the upper portio of the reactor was a cylinder 5 in. ID by 7.3 in. in height Below this was a conical section 6 in. in height with a 2 in. ID discharge port at the bottom.
  • the unit was equipped with two tangential feed nozzles near the top of the cylindrical section.
  • a feed salt having a nominal composition: Na 2 CO 3 -30%, Na 2 SO 3 -50%, a 2 S0 4 -20% was fed through one of the nozzles mixed with powdered petroleum coke.
  • a natural gas/air burner was fired through the secon nozzle. Product melt and gas were discharged through the bottom nozzle. Typical results are given in Table I.
  • a test reactor was constructed of simple cylindrical design in the general shape and configuration of the unit shown in FIG. 1.
  • the inside diameter was 1 ft. and the inside height 6 ft.
  • the unit had one tangential feed inlet and a central burner port at the top.
  • Coal was fed as fuel with air through the central burner.
  • Salt was fed through the tangential feed nozzle together with pulverized coal, using air as the transport gas.
  • the nominal composition of the salt was varied in the two runs as shown in Table II. Typical test results were as follows:

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Abstract

Un composé de sulfoxyde de métal alkalin est converti en un sulfure de métal alkalin correspondant par une réaction avec un matériau carboné solide. La réaction a lieu pendant le chauffage d'un composé de sulfoxyde et d'un matériau carboné donnant lieu à la formation d'un produit en fusion. Les réactifs sont soumis à une force centrifuge et sont repoussés à la périphérie d'une zone de réaction où ils forment un produit en fusion s'écoulant vers le bas dans lequel la réduction du composé de sulfoxyde en sulfure continue. Le produit est récupéré du produit en fusion sortant de la zone de réaction. Dans un mode préférentiel de réalisation, un ou plusieurs réactifs entrent dans la zone de réaction tangentiellement entraînés par un gaz de transport.
EP19820903536 1981-10-26 1982-10-12 Procede de production de sulfures par ecoulement d'une couche en fusion. Withdrawn EP0091948A4 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US31464381A 1981-10-26 1981-10-26
US314643 1981-10-26

Publications (2)

Publication Number Publication Date
EP0091948A1 true EP0091948A1 (fr) 1983-10-26
EP0091948A4 EP0091948A4 (fr) 1984-02-07

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EP19820903536 Withdrawn EP0091948A4 (fr) 1981-10-26 1982-10-12 Procede de production de sulfures par ecoulement d'une couche en fusion.

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EP (1) EP0091948A4 (fr)
JP (1) JPS58501816A (fr)
KR (1) KR880001606B1 (fr)
AU (1) AU552817B2 (fr)
BR (1) BR8207941A (fr)
CA (1) CA1211273A (fr)
ES (1) ES8308803A1 (fr)
FI (1) FI72496C (fr)
IT (1) IT1158024B (fr)
WO (1) WO1983001437A1 (fr)

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DE4135720C2 (de) * 1991-10-30 1994-09-22 Metallgesellschaft Ag Verfahren zur Spaltung von Natriumsulfat oder Kaliumsulfat enthaltenden Stoffen
KR100407195B1 (ko) * 2001-02-14 2003-11-28 가야에이엠에이 주식회사 금속 황화물의 제조방법
KR100407194B1 (ko) * 2001-02-14 2003-11-28 가야에이엠에이 주식회사 금속 황화물의 제조방법
JP6162981B2 (ja) * 2013-03-01 2017-07-12 日本化学工業株式会社 硫化リチウムの製造方法及び無機固体電解質の製造方法
JP2014169196A (ja) * 2013-03-01 2014-09-18 Nippon Chem Ind Co Ltd 硫化リチウムの製造方法及び無機固体電解質の製造方法
JP6097125B2 (ja) * 2013-04-09 2017-03-15 古河機械金属株式会社 硫化リチウムの製造方法
JP6254413B2 (ja) * 2013-10-07 2017-12-27 古河機械金属株式会社 硫化リチウムの製造方法
CN109373335B (zh) * 2018-09-19 2020-06-23 杭州典范科技有限公司 旋风炉及含盐废液燃烧处理方法和硫化碱制备方法
CN115536224B (zh) * 2022-09-28 2023-08-18 中建安装集团有限公司 矿化再生微粉-工业废渣协同固化淤泥自动化设备及方法
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Also Published As

Publication number Publication date
FI72496B (fi) 1987-02-27
WO1983001437A1 (fr) 1983-04-28
AU552817B2 (en) 1986-06-19
FI72496C (fi) 1987-06-08
JPS58501816A (ja) 1983-10-27
AU9129382A (en) 1983-05-05
CA1211273A (fr) 1986-09-16
KR840001931A (ko) 1984-06-07
KR880001606B1 (ko) 1988-08-25
ES516814A0 (es) 1983-10-01
IT8249353A0 (it) 1982-10-25
IT1158024B (it) 1987-02-18
EP0091948A4 (fr) 1984-02-07
ES8308803A1 (es) 1983-10-01
FI832296A0 (fi) 1983-06-22
FI832296L (fi) 1983-06-22
BR8207941A (pt) 1983-09-20

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