EP2710160A2 - Réacteur de récupération - Google Patents
Réacteur de récupérationInfo
- Publication number
- EP2710160A2 EP2710160A2 EP12726861.3A EP12726861A EP2710160A2 EP 2710160 A2 EP2710160 A2 EP 2710160A2 EP 12726861 A EP12726861 A EP 12726861A EP 2710160 A2 EP2710160 A2 EP 2710160A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- zone
- reactor
- recovery
- manganese
- impeller
- 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- Withdrawn
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B47/00—Obtaining manganese
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G45/00—Compounds of manganese
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G45/00—Compounds of manganese
- C01G45/10—Sulfates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/02—Settling tanks with single outlets for the separated liquid
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/60—Particles characterised by their size
- C01P2004/61—Micrometer sized, i.e. from 1-100 micrometer
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
- C02F2101/206—Manganese or manganese compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
Definitions
- the present invention relates to a recovery reactor and process thereof. More particularly, the invention relates to a reactor for recovery of minerals, particularly manganese from effluents and process for recovery of the same. Background of the invention
- Manganese is a common metal found in effluents generated through manufacture of fungicides and other industrial products. It is essential that manganese be recovered from the effluent in an early stage of the treatment so as to avoid choking and scaling of treatment equipment, as well as to avoid potential environmental hazards of releasing such heavy metals into common disposal streams. The recovered manganese can be reused in the industrial manufacturing, thereby decreasing costs of production. Other industrial byproducts obtained on treatment may also be sold commercially leading to further profits as well as maintaining a green environment. US patent application US2009180945 (Mattioli et.
- the resultant crystals obtained are not of a uniform particle size and require further treatment through milling to reduce particle size and to make it uniform.
- the resulting precipitate further causes choking. It is known that a process that results into crystallized manganese having a reduced particle size does not lead to severe choking of the apparatus, thereby increasing the desirability of producing manganese having a reduced and uniform particle size.
- the reactors known in the art have a separate compartment for collection of precipitate generated so as to avoid formation of impurities.
- the separate compartment takes up much space and it can be cumbersome to extract the precipitate from the compartment without additional equipment.
- the present invention provides a recovery reactor that allows for optimum recovery of manganese from effluents, wherein the manganese is obtained in its carbonate form having uniform particle size, thereby eliminating the expensive step of milling that is conventionally required to obtain uniform particle size.
- the apparatus of the present invention is a single unit, and does not incorporate any separate equipment for recovery and removal of the end product.
- the recovery reactor of the present invention is particularly suitable for being employed for the recovery of manganese from the mother liquor during the production process of EBDC fungicides, particularly mancozeb.
- the technical specification for mancozeb stipulates a minimum percentage content by mass of 20% in mancozeb.
- the process known for the manufacture of mancozeb comprises the following three major steps:
- NABAM i.e. the sodium salt of ethylene bis-dithiocarbamic acid is prepared by reacting ethylene diamine (EDA) with carbon disulfide and sodium hydroxide.
- the sodium salt of ethylene bis-dithiocarbamic acid is reacted with Manganese sulfate with agitation.
- Maneb is obtained as yellow crystals in slurry form.
- the said step of reacting the sodium salt of ethylene bis-carbamic acid with manganese sulfate to obtain maneb is carried out at a predetermined manganese concentration.
- the excess MnS0 4 content in the reactor is checked at regular intervals and maintained between 0.5-0.9%. After the complete addition of MnS0 4 , the excess MnS0 4 content should be maintained between 0.6-0.9%.
- washed maneb is reacted with zinc sulfate to form mancozeb.
- the mancozeb product so obtained is dried, in which the moisture content is brought to 10- 12% (spray dryer) and then to less than 1 % (rotary vacuum dryer).
- a recovery reactor comprising: a) a settling zone, which is at a distal end of the recovery reactor, said settling zone comprising at least one outlet to recover settled precipitate;
- reaction zone which has at least one impeller connected to a motor through at least one connecting rod, said reaction zone additionally comprising a plurality of inlet nozzles and a plurality of vertical baffles;
- a calming zone comprising a plurality of horizontal baffles placed at the proximate, central, and distal ends of the zone;
- an overflow zone said overflow zone including at least one outlet nozzle.
- a process for the recovery of manganese using a recovery reactor comprising: a) providing a vertical recovery reactor, said recovery reactor comprising at least a settling zone, at least a reaction zone, at least a calming zone and at least an overflow zone;
- an improved process for the preparation of EBDC fungicides comprising:
- step (c) subjecting the mother liquor obtained in step (b) to a recovery process in a manganese recovery reactor, said recovery process comprising (a) providing a vertical recovery reactor, said recovery reactor comprising at least a settling zone, at least a reaction zone, at least a calming zone and at least an overflow zone; (b) introducing an effluent mixture comprising at least manganese as an impurity and co- introducing an alkaline reactant along with said effluent mixture into the reaction zone of the provided reactor; (c) causing the introduced effluent mixture and alkaline reactant to accelerate upward through the reaction zone, the upward acceleration in said effluent mixture and alkaline reactant being triggered due to rotation of an impeller provided at the bottom portion of the reaction zone; (d) adjusting the impeller rotation to a predetermined frequency such that uniformly sized manganese salt particles are precipitated; (e) collecting the precipitated particles from the settling zone through the provided outlet at the distal end of said settling zone; (f)
- step (d) reacting maneb obtained in step (b) with zinc sulfate to obtain an EBDC fungicide, (e) drying the EBDC fungicide obtained in step (d).
- Fig. 1 is a cross section of an embodiment of a recovery reactor.
- Fig. 2 is a graphical representation of particle size density of precipitated particles at various velocities of the impeller.
- Fig 3 is a graphical representation on the study of particle size distribution of precipitate obtained from a bubble cap type batch process reactor after milling versus the particle size distribution of precipitate obtained from the settling zone of the present invention.
- the present invention provides a vertical recovery reactor comprising at least a settling zone, at least a reaction zone, at least a calming zone and at least an overflow zone.
- the said recovery reactor is a continuous type mixer settler reactor.
- the recovery reactor has vertical tubular structure with a varying circumference such that the circumference of the proximal end which houses the said overflow zone is wider as compared to the central calming zone and the reaction zone.
- the settling zone may be conically shaped and placed at the distal end of the reactor so as to enable collection of precipitate.
- the settling zone comprises at least one outlet for the removal of precipitate.
- the reaction zone is a tubular structure with a uniform circumference attached to the settling zone at its distal end.
- the reaction zone comprises a plurality of inlet nozzles for introduction of industrial effluent and reacting chemicals.
- the reaction zone may also incorporate an impeller that is attached to a motor by means of a rod, wherein the said impeller is a down flow type with variable speed control that can be operated either manually or automatically.
- the reaction zone comprises a plurality of vertical baffles placed diametrically opposite to each other and are placed at a position between said inlet nozzles and the said impeller such that at least one baffle is placed on diametrically opposite ends of the reactor walls.
- the impeller and the vertical baffles help in even micro level mixing of the reactants.
- the impeller speed is adjustable such that the micro-mixing of the effluent mixture and the alkaline reactant is completed.
- the impeller action causes the liquid to rise up, whilst allowing the heavier particles of favorable particle size to settle into the settling zone.
- the impeller is disposed at an end of the reaction zone such that the settling of the particles in the settling zone is promoted.
- the impeller is disposed at a location within the reaction zone and adjusted to rotate at a predetermined velocity such that the settlement of the fine particulates is not affected due to a rotational motion of the impeller.
- the vertical baffles contribute towards ensuring the maximum mixing of the reactants within the reaction zone and prevent back mixing in the reaction zone.
- the placement of the vertical baffles ensures that the reaction is limited to the reaction zone and does not extend into the zones above or below the reaction zone. It has been found that at a predetermined rotational frequency of the impeller, particles having a uniform and desired particle size are produced.
- the calming zone is a tubular structure with a uniform circumference attached to the reaction zone at its distal end and the overflow zone at the proximal end.
- the function of the calming zone is to essentially reduce the speed of the rising liquid and collect random particles of precipitate that may have travelled out of the reaction zone.
- the calming zone comprises a plurality of horizontal baffles placed in the central, proximal, and distal parts of the calming zone.
- at least two of the provided horizontal baffles are downward type of baffles with a center flow aperture adapted to slow down the speed of the reactant mixture.
- the provided central horizontal baffle is a conical type baffle with annular flow.
- the placement of the horizontal baffles creates a curved flow path that allows for particles of a large size to settle down, while at the same time, allowing the upward flowing mixture to travel smoothly into the overflow zone.
- the horizontal baffles also play a major role in collection of smaller particles that may have travelled upwards with the flowing manganese free mixture and in sending these smaller particles back to the reaction zone.
- the overflow zone is tubular structure, wider than the circumference of the calming zone and the settling zone, and is placed at the proximal end of the reactor.
- the overflow zone is attached to the calming zone at its least diameter end.
- the diameter of the overflow zone gradually increases upwards towards the provided outlet nozzle.
- the overflow zone is provided with at least one outlet nozzle which allows the removal of the manganese free effluent mixture, which has almost negligible particulates.
- the recovery reactor is a continuous type of mixer settler reactor.
- the precipitate settled in the settling zone may be withdrawn from the settling zone on a continuous basis or at regular intervals, so as to maintain a particular level in the reactor.
- the impeller may be a down ward type impeller with variable speed control and a range of velocities that can be operated either manually or automatically.
- the velocity or rotational frequency of the impeller may range from 80 to 200 rpm, which has been found to provide uniform particles having particle size in the range of 40 to 160 ⁇ . It has been found that lower or higher rotation frequency of the impeller did not allow adequate separation of the manganese salt from the reaction mixture. Without wishing to be bound by theory, it is believed that at higher frequencies, the increased velocity of the flowing reaction mixture carries away even the heavier particles through the outlet nozzle while lower frequencies did not allow the particles to coalesce to form particles of sufficient size for settling down.
- the provided vertical and the horizontal baffles may be of any non reactive material, the vertical baffles may be preferably made up of a material such as glass.
- the present invention provides a process for the recovery of manganese using a continuous recovery reactor and settler.
- the process comprises providing a vertical recovery reactor, wherein, the reactor may have at least a settling zone, at least a reaction zone, at least a calming zone and at least an overflow zone.
- An alkaline reactant and an effluent mixture which may contain manganese as one of its impurities are simultaneously introduced into the reaction zone of the recovery reactor.
- the introduced effluent mixture and alkaline reactant are accelerated upward through the reaction zone, wherein, the reaction may cause the formation of a precipitate.
- the upward acceleration of the effluent mixture and alkaline reactant is caused due to the rotation of the impeller provided at the bottom portion of the reaction zone such that a change in the rotation frequency of the impeller causes consequential change in the velocity of the reaction mixture through the recovery reactor
- the precipitated particles settle in the settling zone and are recovered from the settling zone through the provided outlet at the distal end of the settling zone.
- the manganese free effluent mixture moves in an upward direction through the provided calming zone into the overflow zone, where it is extracted through at least one outlet nozzle.
- the lighter precipitate particles which may have travelled upwards with the effluent mixture are caused to settle to the lower zones due to the horizontal baffles.
- the alkaline reactant is Na 2 C0 3 , preferably in the concentration of up to 20%.
- the precipitate collected in the settling zone substantially comprises MnC0 3 . The settled particles were found to possess a uniform particle size.
- the concentration of the manganese impurity found in the un-reacted effluent mixture varied from 0 to about 0.5 ppm, and the precipitate obtained from the settling zone contained up to about 90% of recovered Manganese. It was further found that at an impeller frequency of about 80 rpm, the uniform particle size of the precipitate was about 60 ⁇ . It was further found that when the impeller frequency was increased to about 120 rpm, the particle size of the precipitate was around 120 ⁇ . At 150 and 175 rpm the particle size obtained was 90 ⁇ and 160 ⁇ respectively while at about 200 rpm, the particle size obtained was 40 ⁇ .
- the impeller speed ranges between 80 to 200 rpm. More preferably ranges between 120 rpm to about 180 rpm.
- FIG. 1 illustrated is a continuous type recovery reactor and settler as described in Fig.1.
- the present invention relates to a process for recovery of manganese from industrial effluents in the form of MnC0 3 .
- the manganese recovered from effluents may be reused in industrial processes.
- the vertical recovery reactor has settling zone A at the distal end of the reactor, a reaction zone B, a calming zone C, and an overflow zone D.
- the recovery reactor has tubular structure with a uniform circumference at the central section which houses zones B, and C, and the proximal end of the reactor which houses zone D with a circumference that is larger than that of the central section, and at the distal end has an inverted conical structure which houses zone A.
- Zone A has an inverted conical shape and tapers towards the bottom of the reactor to end at outlet G.
- the precipitated end product settles in zone A, from here it can be removed through recovery outlet G.
- the precipitated end product may be recovered from outlet G at regular intervals so as to maintain a particular level in the reactor.
- Zone B is the reaction zone, which has impeller E, wherein in one embodiment of the invention, the impeller E may be a downflow type impeller. Impeller E is attached to motor F by means of rod K, which runs along the entire length of the cylindrical part of the reactor to meet impeller E which may be positioned at the distal end of Zone B.
- Zone B has inlet nozzles 1 and 2 placed diametrically opposite to each other on the walls of the reactor. Inlet nozzles 1 and 2 introduce the reactants into the reactor. The position of inlet nozzles 1 and 2 enable the reactants to be introduced just above impeller E, thus allowing for maximum turbulence and mixing.
- Reaction zone B has vertical baffles 9, 10, 11 , 12 placed below inlet nozzles 1 and 2 on opposite sides of the reactor.
- the vertical baffles may have an elongated structure with variable length for each individual baffle and preferably made of glass.
- the vertical baffles may be attached two each on opposite walls of the reactor.
- impeller E is a down flow type impeller, the particles remain in a suspended form, particles with large particle size settle down into settling zone A, while lighter particles remain suspended. The particle size depends upon the intensity of turbulence which is created by the action of impeller E.
- Zone C is the calming zone and is placed above reaction zone B. Zone C captures escaped precipitated lighter particles that have not settled in the settling zone, for this purpose zone C has three horizontal baffles placed at regular intervals.
- Horizontal baffle 5 is a downward type baffle and is placed at the distal end of zone C, and has a center flow aperture that ensures smaller particles move downward towards the Zone A.
- Horizontal baffle 5 is attached to the body of the reactor by means of gasket J1.
- the central horizontal baffle 6 is a conical type horizontal baffle and creates an annular flow space.
- Horizontal baffle 6 is supported by a plurality of supports placed below the said baffle.
- Horizontal baffle 7 is placed at the proximal end of zone C, wherein, horizontal baffle 7 is a downward type horizontal baffle with a central flow aperture.
- Horizontal baffle 7 is attached to the body of the reactor by means of gasket J2.
- the horizontal baffles 5, 6, 7 may be made from any non reactive material such as glass.
- Zone D is the overflow zone, and makes up the proximal end of the reactor. Zone D has a wider diameter as compared to the central zones B and C. The wider zone helps further decrease the velocity of the reactants moving upwards. The smaller particles that have escaped the horizontal baffles will settle down to the bottom, thus ensuring near total recovery of the precipitate. Zone D has overflow nozzle 8 placed at the side of the reactor wall. Overflow nozzle 8 lets out reaction mixture almost without any precipitate. On reaching zone D, the velocity of the reaction mixture is greatly reduced, this allows for remaining particles to settle down and move towards zone A.
- the recovery reactor in one of the embodiments may be used to precipitate MnC0 3 .
- the effluent may contain industrial effluent containing manganese in its sulphate form as MnS0 4 .
- the effluent is introduced into the reactor along with reactant Na 2 C0 3 through nozzles 1 and 2.
- the reaction may take place on a continuous basis and the volume of effluent added may be regulated through nozzles 1 and 2.
- impeller E begins to stir the reactant mixture at a desired velocity, causing MnCo 3 to precipitate and settle into settling zone A. Through the actions of impeller E, the MnCo 3 obtained has a uniform particle size.
- the turbulence can be regulated by regulating the speed of the impeller so as to obtain various particle sizes
- Vertical baffles 9, 10, 11 , 12 ensure that back mixing does not occur.
- the quantity of manganese recovered from the effluent was about 90 to 95 % and manganese loss may be decreased to about 1 to 0.05%.
- Fig. 2 depicts the particle size density of MnC0 3 , obtained at different intensity of turbulence. It was found that at a specific velocity (frequency) of the impeller E, the particle size obtained was different.
- D10 represents those velocities at which the resultant particles produced were of such size that 10% of the particles pass through a mesh of 3 ⁇ (or are less than 3 ⁇ )
- D50 represents those velocities at which the resultant particles produced were of such size that 50% of the particles pass through a mesh of 30 urn (or are less than 30 urn)
- D90 represents those velocities at which the resultant particles produced were of such size that 90% of the particles pass through a mesh of 300 urn (or are less than 300 urn).
- D100 represents those velocities at which the resultant particles produced were of such size that where 100% of the particles pass through the sieve.
- the velocity of the impeller is ranged between 80 to 200 rpm, so as to acquire a particle size that ranges between 120 ⁇ to 200 ⁇ .
- the walls of the recovery reactor could be made up of stainless steel or glass, or any other non-corrosive material.
- the reactor could be of various sizes depending upon the volume of the effluent generated. Also, the dimensions of vertical baffles 9, 10, 11 , 12 could vary from rectangular to square.
- the reactor is used to treat the effluent with manganese impurity released from the manufacturing units of Ethylenebisdithiocarbamates (EBDCs) compounds.
- EBDCs compounds are selected from the group of mancozeb, maneb, metiram, milnebmancopper, amobam, asomate, azithiram, carbamorph, cufraneb, cuprobam, disulfiram ferbam metam, nabam, tecoram, thiram, urbacide, ziram dazomet, etem, polycarbamate, propineb, zineb and the recovered manganese is reused in said manufacturing units.
- the present invention provides an improved process for the preparation of EBDC fungicides, said process comprising:
- step (c) subjecting the mother liquor obtained in step (b) to a recovery process in a manganese recovery reactor, said recovery process comprising (a) providing a vertical recovery reactor, said recovery reactor comprising at least a settling zone, at least a reaction zone, at least a calming zone and at least an overflow zone; (b) introducing an effluent mixture comprising at least manganese as an impurity and co-introducing an alkaline reactant along with said effluent mixture into the reaction zone of the provided reactor; (c) causing the introduced effluent mixture and alkaline reactant to accelerate upward through the reaction zone, the upward acceleration in said effluent mixture and alkaline reactant being triggered due to rotation of an impeller provided at the bottom portion of the reaction zone; (d) adjusting the impeller rotation to a predetermined frequency such that uniformly sized manganese salt particles are precipitated; (e) collecting the precipitated particles from the settling zone through the provided outlet at the distal end of said settling zone; (f) allowing
- step (d) reacting maneb obtained in step (b) with zinc sulfate to obtain an EBDC fungicide.
- step (e) drying the EBDC fungicide obtained in step (d).
- the recovery reactor of the present invention is particularly suitable for being employed for the recovery of manganese from the mother liquor during the production process of EBDC fungicides, particularly mancozeb.
- NABAM i.e. the sodium salt of ethylene bis-dithiocarbamic acid is prepared by reacting ethylene diamine (EDA) with carbon disulfide and sodium hydroxide.
- the sodium salt of ethylene bis-dithiocarbamic acid is reacted with Manganese sulfate with agitation.
- Maneb is obtained as yellow crystals in slurry form.
- the excess MnS0 4 content in the reactor is checked at regular intervals and maintained between 0.5-0.9%. After the complete addition of MnS0 4 , the excess MnS0 4 content should be maintained between 0.6-0.9%.
- the excess manganese in the mixture of this step of the reaction is recovered using the method as described hereinbefore. The recovered manganese is recycled for further reaction with NABAM.
- washed maneb is reacted with zinc sulfate to form mancozeb.
- the mancozeb product so obtained is dried, in which the moisture content is brought to 10- 12% (spray dryer) and then to less than 1 % (rotary vacuum dryer).
- a fluid bed type of bubble cap crystallizer in semi batch operation was used to treat effluent containing about 3000ppm MnS0 4 , with 9% Na 2 C0 3 . Instead of sludge, crystal pellets of MnC0 3 were obtained. Pallets with an approximate size of ⁇ 250 ⁇ were obtained. The particle size obtained was not uniform. The side draw from the reactor yielded about 50ppm of Manganese which was sent for disposal. The precipitate obtained in the process did not have a uniform particle size.
- the overflow from the reactor was subjected to Inductively Coupled Plasma-Mass Spectrometry to determine quantity of Manganese.
- Fig 3 is a comparison of the particle size of particles obtained from the fluid bed crystallizer after milling and the particle size of the particles obtained from Zone A of the recovery reactor.
- Fig.3 D (Ax10) denotes particle size that could pass through the sieve or the cumulative fraction of particles which are below a certain particle size.
- the particle size of the particles obtained from recovery reactor are below 200 ⁇ .
- Zone A had up to 90% particle size density.
- the invention has been described above by way of illustration, and the specific embodiment disclosed is not intended to limit the invention to the particular forms disclosed. For example, the embodiments described in the foregoing were directed to providing a clear idea about the preferred modes, including the best mode, of making and using the present invention. However, in alternate embodiments, those skilled in the art may implement the invention without deviating from the central idea of the invention. The invention therefore covers all modifications, equivalents, and alternatives falling within the spirit and scope of the following claims
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Inorganic Compounds Of Heavy Metals (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Removal Of Specific Substances (AREA)
Abstract
La présente invention concerne un réacteur de récupération muni d'au moins une zone de sédimentation, d'une zone de réaction et d'une zone de surverse, et un procédé de récupération du manganèse provenant d'effluents industriels par traitement dans ledit réacteur de récupération, ledit manganèse récupéré présentant une taille de particules uniforme.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
IN1539MU2011 | 2011-05-20 | ||
PCT/IB2012/052510 WO2012160494A2 (fr) | 2011-05-20 | 2012-05-18 | Réacteur de récupération |
Publications (1)
Publication Number | Publication Date |
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EP2710160A2 true EP2710160A2 (fr) | 2014-03-26 |
Family
ID=46246110
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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EP12726861.3A Withdrawn EP2710160A2 (fr) | 2011-05-20 | 2012-05-18 | Réacteur de récupération |
Country Status (6)
Country | Link |
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EP (1) | EP2710160A2 (fr) |
CN (1) | CN103562420B (fr) |
BR (1) | BR112013029756A2 (fr) |
CO (1) | CO6811845A2 (fr) |
MX (1) | MX358085B (fr) |
WO (1) | WO2012160494A2 (fr) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
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EP3181220A1 (fr) * | 2015-12-16 | 2017-06-21 | Basf Se | Procédé permettant d'éliminer un catalyseur hétérogène à partir d'un produit de réaction et procédé de production d'une amine aromatique |
CN107118142A (zh) * | 2017-04-26 | 2017-09-01 | 利民化工股份有限公司 | 代森锰铜化合物及其制备方法与应用 |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4544477A (en) * | 1983-10-12 | 1985-10-01 | Standard Oil Company | Polar solvent extraction and dedusting process |
US4994175A (en) * | 1988-12-14 | 1991-02-19 | Amoco Corporation | Syncrude dedusting extraction |
CN2775029Y (zh) * | 2005-04-07 | 2006-04-26 | 凯膜过滤技术(上海)有限公司 | 均相流床反应器 |
CN101314120B (zh) * | 2007-05-31 | 2010-05-26 | 中国石油化工股份有限公司 | 一种浆态床反应器及其应用 |
CN201062279Y (zh) * | 2007-06-15 | 2008-05-21 | 湖北开元化工科技股份有限公司 | 一种回收软锰矿粉的设备 |
US8043585B2 (en) | 2008-01-15 | 2011-10-25 | Vale Inco Limited | Liquid and solid effluent treatment process |
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2012
- 2012-05-18 EP EP12726861.3A patent/EP2710160A2/fr not_active Withdrawn
- 2012-05-18 BR BR112013029756A patent/BR112013029756A2/pt not_active IP Right Cessation
- 2012-05-18 CN CN201280024515.4A patent/CN103562420B/zh not_active Expired - Fee Related
- 2012-05-18 MX MX2013013522A patent/MX358085B/es active IP Right Grant
- 2012-05-18 WO PCT/IB2012/052510 patent/WO2012160494A2/fr active Application Filing
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Also Published As
Publication number | Publication date |
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CN103562420B (zh) | 2016-08-24 |
WO2012160494A3 (fr) | 2013-01-17 |
CO6811845A2 (es) | 2013-12-16 |
WO2012160494A2 (fr) | 2012-11-29 |
BR112013029756A2 (pt) | 2017-09-05 |
MX2013013522A (es) | 2014-05-27 |
CN103562420A (zh) | 2014-02-05 |
MX358085B (es) | 2018-08-03 |
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