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WO2004051166A2 - Deshumidification, sechage et regulation de la grosseur de grains combines de matieres - Google Patents

Deshumidification, sechage et regulation de la grosseur de grains combines de matieres Download PDF

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Publication number
WO2004051166A2
WO2004051166A2 PCT/EP2003/013592 EP0313592W WO2004051166A2 WO 2004051166 A2 WO2004051166 A2 WO 2004051166A2 EP 0313592 W EP0313592 W EP 0313592W WO 2004051166 A2 WO2004051166 A2 WO 2004051166A2
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WO
WIPO (PCT)
Prior art keywords
centrifuge
dryer
solid
gas
particles
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.)
Ceased
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PCT/EP2003/013592
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German (de)
English (en)
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WO2004051166A3 (fr
Inventor
Gabriel Baumann
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Individual
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Individual
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Priority to AU2003302692A priority Critical patent/AU2003302692A1/en
Publication of WO2004051166A2 publication Critical patent/WO2004051166A2/fr
Publication of WO2004051166A3 publication Critical patent/WO2004051166A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/10—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour carrying the materials or objects to be dried with it
    • F26B3/12—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour carrying the materials or objects to be dried with it in the form of a spray, i.e. sprayed or dispersed emulsions or suspensions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/20—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles discharging solid particles from the bowl by a conveying screw coaxial with the bowl axis and rotating relatively to the bowl
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B15/00—Other accessories for centrifuges
    • B04B15/12—Other accessories for centrifuges for drying or washing the separated solid particles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/10—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers
    • F26B17/107—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers pneumatically inducing within the drying enclosure a curved flow path, e.g. circular, spiral, helical; Cyclone or Vortex dryers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B5/00—Drying solid materials or objects by processes not involving the application of heat
    • F26B5/08—Drying solid materials or objects by processes not involving the application of heat by centrifugal treatment
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B7/00—Drying solid materials or objects by processes using a combination of processes not covered by a single one of groups F26B3/00 and F26B5/00
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/20—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles discharging solid particles from the bowl by a conveying screw coaxial with the bowl axis and rotating relatively to the bowl
    • B04B2001/2091—Configuration of solids outlets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B5/00—Other centrifuges
    • B04B5/10—Centrifuges combined with other apparatus, e.g. electrostatic separators; Sets or systems of several centrifuges
    • B04B2005/105—Centrifuges combined with other apparatus, e.g. electrostatic separators; Sets or systems of several centrifuges being a grinding mill
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B2200/00—Drying processes and machines for solid materials characterised by the specific requirements of the drying good
    • F26B2200/18—Sludges, e.g. sewage, waste, industrial processes, cooling towers

Definitions

  • the invention relates to a method and an apparatus for producing a dried, granular or powdery material from a suspension or slurry, for.
  • B. industrial sludges such as gypsum, fine coal, mineral sludge, organic fermenter broths, paint sludge, sewage sludge or the like, in which the continuously added suspension first in a continuously operating centrifuge such.
  • B. solid-bowl screw centrifuge or screen screw centrifuge is mechanically dewatered, at the same time the constantly dewatered thick matter immediately and without intermediate storage and dosing and without leaving the apparatus at least one further treatment such as B.
  • the invention relates to a device for carrying out such a short-term method with a solid-bowl screw centrifuge or sieve screw centrifuge for mechanical drainage inside, a dryer housing which at least partially surrounds the centrifuge, the rotating solid discharge of the centrifuge simultaneously as a metering device and atomizing machine for the pre-dewatered solid in the enveloping
  • the dryer acts, with means for deflecting the particle trajectory in the axial direction of the centrifuge, with at least one hot gas inlet and at least one outlet for the dried solid particles and the drying gas, a pneumatic delivery line, post-drying, a separator with a discharge element for the dried material, and a blower for the promotion of gases, a gas heater, a gas cleaning station and an outlet for the exhaust gas.
  • a method and a device of this type are known from EP 0.591 299 and from DE 196 31 605. 7 - 09 and DE 44-07536 A 1 known.
  • the thick matter particles emerging from the centrifuge at high speed are removed by suitable means, e.g. B. deflected by baffles or by suitable gas flow in the axial direction of the centrifuge.
  • suitable means e.g. B. deflected by baffles or by suitable gas flow in the axial direction of the centrifuge.
  • the sprayed, pre-dewatered solid particles are washed around by the drying gas at a high relative speed and dried very quickly.
  • the drying room is, for example, a stepped concentric annular space. It is made from the outer dryer housing, the rotating drum barrel inside the centrifuge or an inner, formed the rotating drum of the centrifuge surrounding non-rotating housing and the two housing end walls.
  • DE PS 12 17 983 describes a method and the device for this purpose for the heat treatment of a granular or powdery material, in which the already granular, moist material is introduced in a hot air stream, dried in a fluidized bed, ground in a fluidized bed or in a beater mill, sifted and the dried fine material is discharged, the coarser particles advantageously staying longer in the system.
  • DE PS 39 15 082 describes a method and a system for dewatering and drying sewage sludge which consists of many individual devices connected in series with different assigned functions.
  • DE OS 2628 948 describes a method for dehydrating and drying fine, granular products from a suspension, which consists of a mechanical filter and a downstream rotating contact dryer.
  • DE OS 33 40636 a method is shown with device for batchwise combined dewatering and drying in a plurality of series-connected apparatuses, the product must be treated in a long-term but dryer and thereby adversely verändem 'can.
  • OS DE 1 432 864 a device for the production of dry solids from solid-liquid mixtures is known which, after mechanical dewatering, the moist solid, e.g. B. sodium bisulfite, crushed with a rotating splitter before the downstream, operated with hot nitrogen current dryer.
  • US Pat. No. 1,936,866 describes a combination of a screen centrifuge with a centrifugal dryer for dehumidifying and chemically modifying ammonium sulfate crystals. , -
  • DE OS 24 55 312 describes a solid-bowl screw centrifuge with a downstream device for dewatering and washing calcium sulfate hemihydrate, which is produced as a waste product with harmful impurities built into the gypsum and can therefore not be processed in conventional drying processes without a reduction in quality.
  • the plaster is recrystallized from calcium sulfate-alfa hemihydrate immediately after leaving the decanter.
  • Solid-bowl screw centrifuges are successfully used to separate the liquid from fine-grained industrial products with a large specific surface area.
  • the separated solid cake binds relatively large amounts of liquid from the mother liquor, which can only be removed with great effort in downstream washing and drying devices in order to obtain the solid in pure form.
  • the separated fine-grained solid contains a high residual moisture and usually has a sticky, pasty consistency, which often leads to blockages in the downstream transport equipment and apparatus.
  • Another disadvantage of fine-grained suspensions is the small size of the dried particles and their particle size distribution.
  • the small particles with a very large specific surface area produced by the process of particle formation at the solids discharge of the centrifuge allow very short drying times, but larger granules are sometimes required for the storage and further processing of the dried product.
  • single-grain dried sludges tend to generate dust when loading or transporting.
  • the invention is therefore based on the object to avoid these disadvantages and to provide a combined dehumidifier of the type mentioned, in which even with poorly dewatered thick matter, or even with very sticky sludges, no deposits and incrustations can occur in the dryer room, the effort and the costs for the entire treatment, such as mechanical dehumidification, washing, chemical conversion, expulsion of volatile components, drying, avoidance of undesirable side reactions, sanitization, increasing the yield, by means of the short-term treatment in a continuously working multifunction apparatus, and significantly reducing the size of the dried solid particles can be controlled during the drying process.
  • the invention provides for the fine dispersion of the pre-dewatered thick matter in the spray zone of the centrifuge to be uniformly enforced with a high concentration of already dried particles and for these dispersed thick matter particles to be well distributed in the drying gas.
  • the mass of the sprayed damp small particles in the dryer room should be applied evenly to the surface of the drier particles located in and around the spray zone.
  • the dwell time in the spray zone of the particles which increase in size due to build-up granulation and at the same time dry, can be adjusted by the speed of the hot gas.
  • the relative velocity of the hot gas compared to the constantly moistened surface particles should be as large as possible to ensure that the moist, enlarging solid particles in the fluidized bed and during the subsequent pneumatic transport dry very quickly.
  • the active chamber walls in the dryer are designed, for example, outside the rotating centrifuge drum in such a way that a dense fluidized bed is formed around the spray zone and no ejected moist particles hit the dryer walls directly.
  • the fine, moist and sticky particles dispersed by the centrifuge should accumulate on the surface of the constantly moving particles present in the fluidized bed and enlarge them.
  • the flow of the hot gas is specifically influenced by guide and guide plates installed in the dryer room in order to achieve an even distribution of solids and gas, to avoid dead spaces and to ensure intensive contact of the hot gas with the moist, constantly increasing solid particles.
  • Perforated walls through which gas flows are also suitable for preventing wall encrustation in the combined dehumidifying device due to moist, sticky, thick matter particles if the inflowing hot gas keeps the sticky particles away from the walls until the particles on the surface have dried sufficiently and then at a lower moisture content lose their tendency to adhere.
  • the tendency to adhesion is particularly high in certain moisture ranges and, according to the invention, can be overcome in the fluidized bed by granulation in the case of this drying device.
  • the drying room can be divided into zones with different gas velocities in order to specifically influence the particle concentration and the particle sizes in the individual areas of the drying room.
  • the gas distribution and velocity required for the production of the fluidized bed can be designed differently by the inflow surface.
  • the average particle size and the particle size distribution of the dry product can be controlled in a targeted manner by blowing smaller solid particles that have already dried into the spray zone of the centrifuge.
  • the radially outward spray of pre-dewatered fine solid particles continuously generated by the centrifuge hits the large number of surfaces of the blown solid particles in the surrounding fluidized bed.
  • the grain shape can also be influenced in a targeted manner. Smaller dry matter particles from the selective The fluidized bed or sieved fractions of the dry product can be recycled to the vicinity of the spray zone for granulation or introduced with the hot gas.
  • the larger particles formed by the build-up granulation have a higher swarm sink rate and sink downward within the fluidized bed or are preferably in zones with a higher gas upward speed.
  • the larger particles that have sunk into the lower area can preferably be transported out of the dryer room by means of conveying devices in the gas distribution floor.
  • the geometrical design of the zone in the spray area of the centrifuge can ensure that there are primarily smaller particles with a lower swarm sink rate, the diameter of which should be increased.
  • the temperature distribution in the individual fluidized bed areas can also be controlled by introduced hot gases, by heating the wall surfaces or by heating pipes in the fluidized bed.
  • a dry product with large granules can be produced in a targeted manner, without the advantageous combined dewatering and drying in a single machine with very high heat transfer rates and large volume-related evaporation rates.
  • elements protruding from the outside of the rotating centrifuge drum into the dryer space are attached, which light up the gas flow and ensure a strong counterflow and turbulence in the vicinity of the spray zone of the centrifuge solids discharge.
  • fixed or moving baffles with rigid or elastic active surfaces can be installed in the spray zone, which completely or only partially surround the centrifuge discharge zone so as not to obstruct the hot gas flow ,
  • the baffles built into the spray zone can also completely or partially direct the damp fine solid particles sprayed out into other gas-flow zones in order to preferably build up even smaller solid particles or to better distribute the solids in the gas stream.
  • Drum parts of the dewatering centrifuge that are covered by the gas flow as required, for example, with full-screen centrifuges, can be supplied with solid spray mist by targeted particle deflection and a hot gas flow can be passed through them.
  • Extended drying rooms located immediately before, in and above the spray zone of the centrifuge allow selective drying of the larger solid particles by the formation of a circulating fluidized bed.
  • the degree of drying of the solid granules can be further increased by downstream convective flight dryers integrated in the pneumatic conveying line before the separator or long-term transport dryer after the separator.
  • the residence time of the solid and the relative speed to the drying hot gas can be greatly increased by impact surfaces and deflection surfaces in the after-dryer due to the braking effects.
  • the advantages that can be achieved with the invention are, in particular, that instead of a large number of devices and apparatuses for the treatment of fine-grained, industrially produced suspensions and products, a single, compactly constructed multifunctional apparatus is present in a continuous manner of operation and with a high throughput, which is several at the same time be able to carry out ongoing work steps in one apparatus, control the granulate size, increase product quality, prevent incrustation and reduce investment and operating costs.
  • the high heat transfer rates result in a number of advantages, such as low energy consumption, small compact design, small RoJ diameter and apparatus, as well as low investment and operating costs.
  • the possible dryer volume can be made relatively large despite the small centrifuge, since the dryer housing according to the invention is independent of the total length of the inner dewatering centrifuge.
  • the evaporation capacity is adapted to the high product throughput of the centrifuge. Due to the cross flow of the solids discharge of the centrifuge, the performance and size of the dryer can also be adapted to the requirements regardless of the size of the dewatering centrifuge.
  • the entire evaporation capacity of the drying system is no longer provided by the combination machine alone.
  • the downstream post-dryer and the pneumatic transport using hot gas in the lines also provide part of the dryer performance of the system.
  • the multifunction machine generally handles the difficult drying sections of the glue phase. overcome without backmixing of additional substances.
  • Another advantage is that existing sludge centrifuges for only dewatering can be retrofitted in the usual design of full-shell centrifuges or screen screw centrifuges in the manner according to the invention to multifunction machines in which mechanical dewatering, drying and granulation can be carried out.
  • the invention nuances the advantageous dispersing properties of continuously charged and spraying centrifuges (which include solid bowl screw centrifuges, solid bowl nozzle centrifuges, sieve screw centrifuges or nozzle separators). are) as an atomizing machine, so that, according to the invention, a sludge centrifuge is now assigned two main functions instead of the previous, sole separation function: firstly, the mechanical separation of thick matter from the suspension, and secondly the dispersion and atomization of the separated thick matter into the smallest particles and their distribution and drying by a stream of drying gas.
  • This second function namely the advantageous use of the fine dispersing properties of the thick material discharge of a sludge centrifuge in the construction z. B. a full jacket centrifuge, has not been used technically for the purpose of spray drying.
  • FIG. 1 shows the longitudinal section of a combined centrifuge dryer with a solid-bowl screw centrifuge as an atomizing machine, with a solid fluidized bed around the entire centrifuge drum.
  • FIG. 2 shows the combined centrifuge dryer from FIG. 1 in cross section
  • FIG. 3 shows a combined centrifuge dryer with all additional system parts and peripheral devices.
  • FIG. 4 shows a combination of a solid bowl centrifuge with a flow-through dryer with solid enrichment only around the spray zone of the decanter.
  • FIG. 5 shows a combined centrifuge dryer with a vertically arranged decanter as a spraying machine in the fluidized bed with an overflow weir for the solid.
  • Fig. 6 shows a cross section of a combined centrifugal dryer bode ⁇ as a combination of solid shedding a solid bowl screw centrifuge with a circulating fluidized bed dryer without perforated plate 'and solid baffles.
  • FIG. 7 shows an aniagram for self-inerting cycle gas operation with a centrifuge dryer and pretreatment of the suspension by external dry material backmixing.
  • FIG. 8 10 shows a schematic longitudinal section of a combined centrifuge dryer as a combination of the solid discharge of a screen screw centrifuge with two different filtrate outlets and a combination of different impingement cones.
  • FIG. 11 shows a longitudinal detail view for the thermal expansion-appropriate mounting of the combined centrifuge dryer on the centrifuge frame and for sealing the dryer housing against the rotating centrifuge components.
  • FIG. 12 shows a longitudinal section through the spray zone of the combined centrifuge dryer as a multifunction machine with a dispersing aid through a fan wheel with pin mill and rear-ventilated baffle cone.
  • FIG. 13 is a view of the completed system of a combined centrifuge dryer with a circulating fluidized bed dryer, with a second after-dryer before and a granulating device for the product after the cyclone separator.
  • the combined centrifuge dryer shown in longitudinal section in FIG. 1 and in cross section in FIG. 2 is a dewatering and drying machine and has a solid-bowl screw centrifuge 1 of a known type.
  • the solid-bowl screw centrifuge also serves as an atomizing machine for the pre-dewatered solid and is surrounded by a solid fluidized bed around the entire centrifuge drum 1. The outside is cleaned automatically by centrifugal force.
  • other centrifuges suitable for dewatering for example sieve-shell screw centrifuges, solid-shell nozzle centrifuges, 3-phase separation centrifuges or separators, in which the separated solid phase is then to be dried, can be used.
  • the solid-bowl screw centrifuge 1 which is referred to below as an example of a dewatering centrifuge, has a rotating drum shell 2 which is rotatably supported at its axial ends on roller bearings 3.
  • the drum shell 2 tapers conically at one of the two ends and is at a " fine tapered end with discharge openings. 4, which forms the discharge zone 5 for the pre-dewatered thick matter 6.
  • the liquid sludge 8 fed into the interior of the centrifuge 1 through a sludge pipe 7 is separated into a thick matter 6 and a clarified liquid 9 in the centrifuge 1 due to the centrifugal force . which at the other end of the drum jacket 2 is sprayed out of the centrifuge 1 into a separate housing, the centrate chute 10.
  • the dryer directly surrounding the centrifuge 1 is through an outer dryer housing
  • the drying gas 15 is through hot gas lines 16 from below under the Fluidized bed 17 initiated.
  • the fluidized bed 17 consists of a perforated sheet with round or slot-like holes through which the hot gas 18 flows.
  • the pressure drop occurring when flowing through should be so great that the hot gas 18 enters the dryer chamber 19 evenly in the longitudinal and transverse directions.
  • the free hole-area ratio of the fluidized bed 17 is normally chosen so that there is a pressure drop which corresponds approximately to the pressure loss of the fluidized bed itself.
  • the evenly entering hot gas 18 flows around and penetrates the thick matter 6 dispersed in the form of fine particles through the entire circumference through the decanter solid discharge openings 4.
  • a bubbling gas-solid fluidized bed forms in the entire dryer space 19, which flows over the rotating solid bowl centrifuge 1 from the outside and encloses it.
  • an impeller 20 is attached to the rotating drum jacket 2 next to the discharge zone 5, which hot gas in the direction of the solid Spray 6 blows and deflects it in the axial direction.
  • the solid spray mist 6 dispersed into the fluidized bed is deposited on the already dried particles of the fluidized bed in motion and increases these particles.
  • the hot gas 18 dries the externally moistened particles very quickly, since a large specific surface area of the solid particles 6 is available for heat and material exchange.
  • the gas 21 emerging at the upper edge of the bubbling fluidized bed and cooled by the drying is collected in the upper region of the dryer housing 11 and suctioned off at the suction pipe 22.
  • the lighter, smaller particles and the dust are discharged with the gas 21.
  • the hot gas 15 introduced at 16 from below is distributed through the inclined fluidized bed floors 17 according to their free hole cross section and flows into the dryer chamber 19 at different gas velocities 8. Sinking larger particles automatically pass through the inclined position of the perforated fluidized bed floors 17 into the transport screw 24 which is not or only slightly flowed through by the gas and is discharged.
  • the upward velocity 47 of the gas in the fluidized bed can be designed by the angle of inclination and the perforation of the two fluidized bed bottoms 17 such that large, dried, large particles that reach the conveyor screw 24 only through built-up granulation.
  • the size the sinking particles 23 can be controlled via the speed of the gas 18.
  • the dryer housing 11 can be extended upwards in a manner not shown instead of the vertical walls.
  • a side opening with an adjustable overflow weir can also be provided in the end wall 14 as an additional solids outlet.
  • Standing, moving or rotating impact surfaces or deflection surfaces 25 can also be installed around the discharge zone 5.
  • a combined centrifuge dryer completed with other plant parts and peripheral devices is shown as an example.
  • the centrifuge dryer consists of the centrifuge rotor 1, which is partly built into the dryer, with an outlet 10 for the mechanically separated centrate liquid 9 and a solids discharge zone 5 at the other end.
  • the dryer housing 11 is divided into four sections in the axial direction.
  • the first section 26 in the vicinity of the solid spray zone 5 serves to introduce dried solid particles mixed with carrier gas, which are constantly wetted externally by the moist solid spray 6 of the centrifuge 1.
  • the introduced dry matter granules ensure that the spray mist 6 is constantly surrounded by absorbent dry, free particles of the fluidized bed.
  • the moist spray mist 6, which is enveloped by particles, cannot be sprayed directly onto the dryer walls, it is shielded by the fluidized bed.
  • the second section 27 of the dryer housing 11 is used to introduce hot gas 18 into the fluidized bed, which is made uniform in its entry speed by the perforated fluidized bed floor 17.
  • hot gas 18 is also introduced, the temperature or empty pipe speed of which may, however, be different.
  • cooled gas 21, mixed with dried solid particles 30, is drawn off from the fluidized bed space 19.
  • the circulating gas blower 31 ensures the solids circulation of dried grains 30 in the centrifuge dryer from 29 to 26, and on the other hand also for the transport of at least some of the dried solids grains to the separator 32, which is shown as an example as a cyclone.
  • the freed from the solid air 33 is supplied to the scrubber 35 to a smaller extent by the fan 34.
  • the larger proportion of the dust ten exhaust gas 36 is mixed with hot flame gases 37 again sucked in by the blower 38 and pressed again into the centrifuge dryer 11.
  • the hot flame gases 37 are generated in the gas heater 39 by a burner 40 which burns the fuel 41 with a low excess of pollutants.
  • Part of the scrubbed exhaust gas 43 is reintroduced as a low-oxygen cooling gas 44 around the burner 40 to the gas heater 39 and thus returns to the gas cycle.
  • the excess gas portion 45 is blown off the system through the chimney as dedusted and washed exhaust gas 46.
  • the water evaporated in the centrifuge dryer 11 is condensed in the washer 35 by cooling and discharged with the washing water 48 and removed from the dryer circuit.
  • the constant supply of oxygen-poor flame gases 37 and the removal of moist exhaust gases 45 from the drying system result in a circulating gas atmosphere 33 which is greatly depleted in the oxygen content by CO 2 self-inerting. This prevents dust explosions and spontaneous combustion of dry products at risk of fire.
  • the dry product 30 separated in the separator 32 is discharged, for example, via a cellular wheel sluice 50.
  • the larger granules 23 formed in the dryer chamber 19 sink to the fluidized bed 17 and are discharged from the dryer by the conveyor screw 24 and the discharge lock 51.
  • the two Tock products' coarse pellets 52 and 53 smaller pellets can be mixed together, or further processed separately for different purposes.
  • the pellet sizes can be specifically controlled by the possible setting parameters and produced in the desired grain sizes.
  • Fig. 4 shows schematically in longitudinal section a combination of a solid bowl centrifuge 1 with a centrifuge dryer, in which only the solids discharge and spray zone 5 of the centrifuge 1 is integrated into the surrounding centrifuge dryer 11.
  • a hot gas stream 15 is directed from below the solid spray 6 radially ejected by the centrifuge 1 in order to brake the solid particles rapidly downwards.
  • rotating self-cleaning impellers 20 are attached to the outside, which constantly suck the gas sideways at the solids discharge openings 4 and generate a strong negative pressure at the discharge zone 5.
  • the negative pressure 55 in relation to the surroundings of the dryer chamber 19 causes gas laden with particles to flow rapidly from the fluidized bed in the discharge zone 5 radially from the outside inwards, which is directed in the opposite direction from the sprayed solid spray 6 with its moist and sticky particles.
  • the moist solid particles are braked very quickly, coated and dried in a very short time. Due to the very high relative speed that occurs, extremely high heat and mass transfer rates are achieved. As a result, the specific water evaporation capacity and volume-related dryer capacity are greatly increased. These transmission powers cannot be achieved in a normal fluid bed dryer.
  • the relative speed between hot gas and moist particles in a normal fluidized bed dryer according to the prior art is approximately 1-2 m / s, whereas relative speeds of 30 to 60 m / s are achieved in this arrangement according to the invention.
  • the centrifuge dryer Due to the geometrical design and the corresponding gas velocity, the centrifuge dryer can be operated in continuous operation with a single gas passage, but it can also be operated with a side gas and product outlet in cycle gas operation. If the gas-permeable perforated plate 17 is omitted in order to equalize the speed of the incoming drying gas 15 as in FIG. 6, the opening angle 54 of the dryer housing 11 above the hot gas line 16 must be reduced and the centrifuge dryer builds higher.
  • FIG. 5 shows a centrifuge dryer with a vertically arranged solid bowl screw centrifuge 1 as a solid spraying machine in the fluidized bed.
  • a nozzle decanter or a nozzle separator with a vertical axis could also be installed.
  • the solid bowl screw centrifuge 1 is supported by the two roller bearings 3 below and above.
  • the frame 66 for the upper bearing 3 is guided as an axis cross through the solid fluidized bed.
  • the solid-bowl screw centrifuge 1 is supplied with the liquid sludge 8 via an insulated line 7.
  • the separated liquid 9 flows out at the bottom via a center chute 10, the pre-dewatered solid is flung out of the solid discharge openings 4 as a solid spray 6 at the top of the fluidized bed.
  • the fluidized bed dryer shields the walls 11 from the wet spray '6 by the many moving particles.
  • the hot gas 15 is pressed in from below through insertion shafts 16 under the fluidized bed 17 and enters the fluidized bed 19 at a uniform rate at 18. Heat is again supplied to the hot gas, which cools due to water evaporation, through heating pipes 55 located in the fluidized bed, and heat is also transferred through the heating pipes 55 to the contacting solid particles. This measure significantly increases the volume-related evaporation rate.
  • the smaller, dried solid particles 53 are discharged via a height-adjustable overflow weir 56.
  • the dust-containing exhaust gas 21 leaves the centrifuge dryer through the suction pipe 22.
  • Coarser particles 52 that have sunk into the fluidized bed can be removed by a slit weir directly above the fluidized bed bottom 17.
  • the height of the fluidized bed 58 is highest near the spray zone 6, in the direction of flow towards the dryer outlet 56 ne 6 highest, in the direction of flow towards the dryer outlet 56, the layer 58 becomes somewhat lower due to a slope.
  • FIG. 6 shows in cross section a combined centrifuge dryer as a combination of the solid discharge of a solid bowl screw centrifuge 1 with a circulating fluidized bed dryer 11 without perforated plate bottom.
  • the centrifuge dryer shown is constructed similarly to that in Fig. 4, however, the circulating fluidized bed 59 which is formed is mainly above the centrifuge rotor 1.
  • the velocity of the hot gas 15 entering at 62 is so high that all follow pre-dewatered solid particles 6 thrown off at the bottom are immediately carried upwards by the hot gas 15.
  • the dryer housing 61 around the solids discharge zone 5 is constructed like the diffuser part of a gas venturi nozzle and is open at the top. The narrowest point in the Venturi nozzle 62 for the hot gas 15 replaces the perforated plate base 17 for the fluidized bed.
  • a circulating fluidized bed 59 is formed in the upper conically expanded dryer section 63.
  • the larger or even wetter and thus heavier solid particles 52 in the upper dryer part 63 reverse their upward direction of movement due to the greatly slowed gas speed and they fall down again into the dryer part 61 with a higher upward speed.
  • This statistically running circulation movement for heavier particles 52 continues until the particles 53 are sufficiently dried, lighter or decayed and are also discharged upwards at 22 and are pneumatically transported in the subsequent pipeline 64.
  • the part of the dryer housing 61 built around the centrifuge rotor 1 is separated from the other parts of the dryer housing 63, 16 by the two elastic compensators 65 in order to allow thermal expansion and to transmit no vibrations from the centrifuge 1 into the adjacent system parts.
  • FIG. 1 A detailed front view of the combined centrifuge dryer for the thermal expansion-appropriate mounting of the dryer housing 61 of the combined centrifuge dryer on the centrifuge frame 66 is shown.
  • the conically expanded dryer housing 61 expands greatly when the dryer heats up compared to the components 1 and 66 of the dewatering centrifuge which remain cold.
  • the dryer housing 61 consisting of the conical walls 61 and the two side walls 13 and 14, which are sealed against the rotating components of the centrifuge, should move in its central position relative to the axis of rotation 67 and along little along despite all-sided expansion. It is therefore connected to the cold, rigid frame 66 of the centrifuge by laterally flexible support elements 68.
  • the spring elements 68 cause lateral restoring forces which the dryer housing 61 despite keep stretch in its original center position to the turning center.
  • Wound steel springs, rubber springs, vertical bending bolts, or vertical or inclined leaf springs can serve as laterally resilient support elements 68.
  • the natural frequencies of the housing support 68 must be coordinated in terms of vibration so that resonance vibrations and movements cannot occur when the centrifuge 1 is started, operated and switched off. In the zones 70 with the smallest distance of the solid discharge zone 6 from the
  • Dryer walls 61 in addition to the elements described in FIG. 11, can be installed in the discharge zone 5, rigidly supported rigid baffles 60, or elastic, resilient or oscillating baffles 69, which clean themselves from solid encrustations.
  • the flat or curved baffles 60, 69 can also be installed at an angle to the spray level of the solid discharge or, like the encrusted dryer walls 61, 16, 63, 13, 14, can be set in a cleaning vibration by a drive 71.
  • these can be flowed behind and perforated, vibrate, guided gas flows or targeted gas jets can also be used.
  • FIG. 7 shows a system diagram for self-inerting cycle gas operation with a centrifuge dryer 49 with a circulating fluidized bed according to FIG. 6 and a pretreatment of the suspension 8 by external dry material backmixing 73 into the liquid sludge.
  • the centrifuge dryer 49 consists of the dewatering centrifuge 1 or 87 and is supplied with hot gas from below by the hot gas generator 39 with burner 40 via the tube 16. The dried product is transported through the suction pipe 22 to the cyclone separator 32, where it is discharged from the gas cycle.
  • the dedusted exhaust gas 33 is conveyed from the circulating gas blower 31 into an exhaust gas component 43 to the scrubber 35 and into a circulating gas component 36 again to the hot gas generator 39 and mixed with the flame gas 37 from the combustion to form the drying gas 15. If the dried product 30 fails, the fine fraction 75 and dust of the product 30 are sucked off by cross air 76 and transported to a separator 77, which is shown as an example of a cyclone, but also z. B. operated a dust filter or a scrubber with liquid sewage sludge can be. The continuously occurring fine fraction 75 separated in the separator 77 is continuously mixed into the suspension 8 through the discharge lock 51.
  • the suspension enriched with the granular dry substance which promotes drainage can also be added with precipitation or flocculation aids 78 in the centrifuge 1, 87 for better clarification by wet mechanics.
  • the dedusted exhaust air 79 is also fed to the scrubber 35 for final cleaning.
  • the exhaust fan 34 sucks the entire Exhaust gas quantity 45 to the chimney 80.
  • the suitable proportions of exhaust gas quantity can be controlled via control flaps 81.
  • the CO 2 self-inerting and condensation of the moisture takes place in a manner similar to that described in FIG. 3.
  • a combined centrifuge dryer with a rotating fluidized bed and internal continuous material return is shown in longitudinal section in FIG. 8 and in the associated cross section in FIG. 9.
  • the hot gas 15 enters in several longitudinal sections 27, 28 through tangentially arranged insertion shafts 16 between the dryer housing 11 and the cylindrical or frustoconical perforated fluidized bed cylinder 83. Due to the tangential inflow process and the type of perforation of the screen cylinder 83, in the form of slots, beads, Conidurblechen or, for example, Gridboden- shaped inlet openings, the tangential inflow of the hot gas 18 and its rotation is forced inside. The pre-dewatered solid is sprayed through the discharge openings 4 of the rotating drum 2 at one end of the drying room.
  • a conical or bowl-shaped baffle plate ring 84 is on the end wall 13 or on the drum. 2 attached, which deflects the spray in the axial direction.
  • a rotating gas-solid fluidized bed 85 is formed within the cylindrical perforated plate 83 and is carried by the inflowing rotating hot gas 18.
  • the layer thickness 86 of the rotating solid fluidized bed 85 which forms depends on the grain sizes, the centrifugal field strength, the gas entry speed, the transport speeds in the axial and tangential directions and the centrifugal swarm density.
  • the solid spray 6 is sprayed onto the rotating fluidized bed 85 from the inside and enlarges the already rotating solid particles.
  • the heat and mass exchange rates achieved in the rotating fluidized bed 85 are much higher than in a fluidized bed in the earth's gravitational field.
  • the fluidized, rotating fluidized bed 85 migrates in the axial direction through the dryer to the suction pipe 22 at the end of the dryer.
  • dry particles are drawn off at 29 and returned to the fluidized bed at 26.
  • the trigger 29 and the introduction 26 can also take place in the tangential direction.
  • the solid blower 31 takes over the return transport of the gas-solid mixture.
  • FIG. 10 shows a schematic longitudinal section of a combined centrifuge dryer 49 as a combination of the solid discharge of a sieve screw centrifuge 87 with two different filtrate outlets.
  • the screen centrifuge dryer 49 consists of the centrifuge rotor s 91 projecting into the dryer with its solids discharge 4, with an outlet 10 for the mechanically separated clarifying centrate liquid 9, the conically shaped housing 93 for the sieve filtrate 92 and a solids discharge zone 5 at the end of the sieving zone 91.
  • the housing 11 of the centrifuge dryer 49 is divided in the axial direction into several sections for hot gas introduction 16, product outlet 61, sieve filtrate housing 93, centrate chute 10.
  • the suspension 8, if necessary mixed with precipitant 78, is added to the sieve screw centrifuge 87 through an inlet pipe 7 and enters the rotating separation space at 88.
  • the clarifying filtrate 9 is injected into the centrifuge chute 10 via direct-flow centrifuges 87 in the case of direct-current centrifuges, and via counter-flow centrifuges directly through the end wall openings.
  • the pre-dewatered solid transported from the screw 89 on the cone inwards to the sieve part 90 of the centrifuge drains 91 further residual liquid on the rotating sieve.
  • This so-called sieve filtrate 92 is thrown out through the sieve 91 into the sieve filtrate housing 93 and flows off at 92.
  • the screen screw centrifuge 87 is able to mechanically dehumidify very large solid mass flows, provided the fine-grained solids can be retained by the rotating screen 91.
  • the solid tasted through the sieve 91 is thrown out at the solid discharge 4, agglomerates are crushed at the armored rotating impact cone 103, distributed in the circumferential direction and somewhat deflected and comes into contact with the inflowing hot gas 15 at 107 in the discharge zone 5.
  • the baffle cone 84 which is flowed behind is exemplified here as a combination of a rotating baffle cone 103 for the distribution in the circumferential direction and an outer, non-rotating deflection cone 84. All sprayed solid particles 6 are carried upwards into the dryer 19 and the speed in the upper dryer diffuser part 63 is slowed down, similar to that in FIG. 6.
  • the rotating sieve 91 can be designed as a cylindrical or slightly conical sieve basket.
  • the slope of the screw conveyor 89 can be less in the sieve part 90 of the centrifuge than in the solid casing part 2. Washing liquid or superheated steam 82 or hot gas can be introduced inside the screen basket 91 in order to improve the mechanical dehumidification in the screen part 91 and to preheat the solid 6 for the subsequent drying.
  • the screen screw centrifuge which is mostly used in processing technology, is capable of mechanically mechanically adjusting very high solids mass flows of approx. 50 1 / h and more to high TR - Values of e.g. B. with coal to dehumidify approx.
  • a non-illustrated race track with a tangential solid outlet upwards or with partial shielding on the sides or downwards according to the prior art can also be attached to the solids discharge 4 in a targeted manner.
  • the particles 6 come into contact with the inflowing hot gas 15 at a high relative speed of 50-80 m / s in the discharge zone 5 and dry off the surface very quickly in milliseconds. All sprayed solid particles 6 are carried upwards into the dryer 19 and then greatly slowed down to approx. 5-15 m / s.
  • the applicable temperatures of the entering hot gas 15 are very high up to 500 ° C., since the rotating centrifuge rotor is thermally very well shielded by the diffuser-dryer housing 61 and the conical screen filtrate housing 93.
  • the hot dryer housing 61 is mechanically completely decoupled from the dryer components für by the elastic expansion compensators 65 and is shielded by the heat insulation 95.
  • the hot dryer housing 61, 94 is also thermally separated from the cold screen filtrate housing 93.
  • a washing nozzle device 96 is fitted inside the screen filtrate housing 93.
  • Fig. 11 shows a longitudinal detail view from a construction drawing similar to Fig. 4, 6, 10, for thermal expansion-appropriate support of the combined centrifuge dryer 49 on the centrifuge frame, for sealing the hot housing walls .13 and 14 of the combined centrifuge dryer 49 against the rotating centrifuge components and Distribution of the solid spray 6 over the entire dryer cross section.
  • the labyrinth carriers 99 are screwed rigidly to the centrifuge frame 66 and carry the non-contact labyrinth seals 100 which are set against the rotor parts with a narrow gap.
  • the labyrinth supports 99 like the roller bearing housings 3, are rigidly connected to the supporting centrifuge frame 66, as a result of which the narrow, contact-free labyrinth gaps 101 do not change even during thermal expansions or movements of the dryer housing 13, 14, 61, 94 or the rotating rotor surfaces of the centrifuge 1, 87 can touch.
  • the hot, expanding dryer housing 13, 14, 61, 94 is fastened to the cold centrifuge frame 66 by means of, for example, 4 laterally resilient bolts 02, so that despite thermal expansion of the hot dryer housing similar to that described in FIG. 6, the narrow labyrinth gaps 101 remain constant.
  • a two- or multiple-action rotating impact device 103 is arranged above the individual solid waste Throw holes 4 attached. Due to the multiple impact and deflection of the trajectory of the solid particles 6 after leaving the discharge openings 4 on impact surfaces 103 connected in series, larger clumps of solid are more easily comminuted and the spray mist is better distributed in the circumferential direction.
  • the impact and deflection device 103 can be arranged concentrically one above the other on the entire circumference in the radial direction, or a single impact and deflection plate 104 with different directions and angles 105 is attached above each discharge opening 4 of the centrifuge rotor 1.
  • the various discharge openings 4 can be distributed not only on the circumference, but also in the axial direction over the flow cross section of the dryer.
  • the impact and deflection device 103, 104 can be a combination of a plurality of deflection elements, which all rotate or consist of a combination with alternating rotating and non-rotating impact elements.
  • the deflection angle 105 of the individual impact elements 104 can be designed differently for each impact element 104 in order to improve the spatial distribution of the solid mist sprayed from the centrifuge drum at 4.
  • the deflection surfaces can also be aligned in the axial direction, rotated to this, in or opposite to the direction of rotation, in order to achieve the best possible spatial volume distribution of the sprayed solid mist in the hot gas flowing through.
  • Each individual discharge opening 4 for the solid 6 can be operated by at least one impact element for directional deflection.
  • the impact surfaces 104 may have applied wear protection in the form of attached hard material plates or welded-on layers.
  • the solid spray 6 can be carried along well distributed in the drying room by the drying gas 15 and can be dried further above the rotor 1, 87.
  • Fig. 12 shows a longitudinal section through the spray zone 5 of the combined centrifuge dryer 49 according to FIGS. 4, 6, 7, 10, 11, as a multifunction machine with an additional dispersing aid through an impeller 20 with pin mill 106 and impact cone 84 and second hot gas inlet 18 through the downward, non-rotating baffle cone 84.
  • additional comminution of the ejected solid particles 6 is advantageous.
  • the subsequent comminution of the solid particles 6, which is superimposed on the drying process constantly creates a new surface which is exposed to the inflowing hot gas and leads to rapid drying of even very poorly dewatered products.
  • the baffle cone 84 which is open at the bottom, additionally guides a portion of the drying gas 15 flowing in from below through the annular gap 107 into the discharge and comminution zone 5.
  • the ratios of the two drying gas quantities 15, 18 flowing in from below can be varied. It can also be, for example, the partial stream 18 a hot gas stream loaded with solid dust 75, the solid of which is used for coating and enveloping the sticky solid particles 6 in order to change their adhesive properties.
  • a pin mill 106 with two fixed pins and one row of pins rotating with the fan blades 20 is shown here as an example of the comminution unit. Of course, several rows of pins can also be arranged. In special cases, the comminution unit 106 can also be omitted and the rotating fan blades 20 with the opposite conveying direction increase the suction through the annular gap 107 and, in an extended form, themselves act as a comminution and scraping tool for the incrustations on the impact cone surface 84.
  • FIG. 13 shows a view of the completed system with a very high throughput of a combined centrifuge dryer 49 with a circulating fluidized bed dryer 63, with a second after-dryer 108 before - and a press granulating device 109 after the double cyclone separator 32.
  • the product-laden gas stream 21 is deflected several times.
  • the solid particles 6 with a mass density thousands of times greater than the gas follow the deflection movements only in part. They hit the wall on the outer channel surfaces 110 and are braked sharply. They reflect there again and cross the hot gas flow 21 at a high relative speed before each new impact. Due to the high relative speed of the particles 6 to the drying gas 21 of approximately 20 m / s, the drying speed of the solid particles 6 is more than tenfold compared to the subsequent drying in a pneumatic delivery pipe - Dryer according to the state of the art. The residence time of the solid 6 in the post-dryer 108 shown is increased drastically.
  • the drying is particularly intensive.
  • the particle distribution in the drying gas 21 over the preferably rectangular channel cross section is improved.
  • the formation of highly concentrated product strands in round pipe cross sections, which has been very damaging to the drying speed up to now, is prevented according to the invention even with large pipe dimensions.
  • a cleaning flap 72 is provided on the lowest elbow after the downward part.
  • the pneumatic delivery pipe is again at the level of the cyclone inlet.
  • This Zig-Zag night dryer 108 is very effective, because of the simply bent sheet metal walls 1.10 very inexpensive to manufacture and easy to integrate into the system.
  • the subsequently dried product 30 is then separated off in the double cyclone 32 shown and discharged from the gas cycle through the rotary valve 50.
  • the powder 30 is transferred directly from the cellular wheel sluice 50 to a press granulator 109, which forms cylindrical pressings 52 from the powder, which are transported away by the transport screw 24.
  • the dedusted drying gas 36 as described in FIGS. 3, 7, is again largely supplied to the hot gas generator 39 by the circulating gas blower 31. A small part is fed to the scrubber (not shown) as exhaust gas 43 and then released into the environment as chimney gas 45.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Drying Of Solid Materials (AREA)
  • Treatment Of Sludge (AREA)

Abstract

L'objectif de l'invention est de produire, à peu de frais d'appareillage et d'énergie, des granules plus grosses à humidité résiduelle réduite, par séchage de liquide épais collants, pouvant être faiblement déshydraté. A cet effet, une centrifugeuse est intégrée dans un logement de séchoir et située dans un dispositif combiné de déshydratation et de séchage, de sorte qu'au moins une partie d'évacuation de déchets de la centrifugeuse est placée directement dans le logement de séchoir et que les particules humides du brouillard de fines gouttelettes de matières projeté de la centrifugeuse atteignent directement, de manière bien répartie dans l'espace, les particules sèches du lit fluidisé à envelopper et à faire circuler, après de nombreux retournements. Le temps d'arrêt momentané dans la zone de pulvérisation des particules, destinées à être grossies par granulation de constitution et à être séchées simultanément, est variable en fonction de la vitesse du gaz chaud. Le flux gazeux chaud est influencé de manière ciblée par des éléments d'impact et des conducteurs, de façon à répartir la matière et le gaz de manière uniforme, ce qui permet d'éviter les zones mortes et de favoriser un contact intensif entre le gaz chaud et les particules de matière qui grossissent continuellement. Selon l'invention, les particules de liquide épais humides, prédeshydratées mécaniquement dans la centrifugeuse, puis dispersées finement, sont réparties uniformément dans le gaz de séchage contenant de la matière, et elles ne sont pas mises en contact prématurément avec les parois du séchoir. Les particules fines, séchées sont grossies par granulation de constitution et le séchoir comprenant une centrifugeuse est protégé de l'encrassement par des produits collants sans reconversion ou par prétraitement des boues.
PCT/EP2003/013592 2002-12-04 2003-12-02 Deshumidification, sechage et regulation de la grosseur de grains combines de matieres Ceased WO2004051166A2 (fr)

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DE10256674A DE10256674A1 (de) 2002-12-04 2002-12-04 Kombinierte Entfeuchtung, Trocknung und Korngrößensteuerung von Feststoffen
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CN101726160B (zh) * 2009-11-10 2013-04-17 中国烟草总公司郑州烟草研究院 一种分散物料气流干燥装置
RU2607445C1 (ru) * 2015-12-14 2017-01-10 Олег Савельевич Кочетов Гранулятор кипящего слоя
RU2647003C1 (ru) * 2017-06-29 2018-03-13 Олег Савельевич Кочетов Сушилка для растворов и суспензий
RU2647921C1 (ru) * 2017-06-29 2018-03-21 Олег Савельевич Кочетов Распылительная сушилка со встречными закрученными потоками типа взп
CN113070154A (zh) * 2021-03-09 2021-07-06 上饶中材机械有限公司 一种高效除尘的水泥熟料输送机
EP3737900A4 (fr) * 2018-01-16 2022-03-16 Waister AS Système modulaire et procédé de séchage de solides et de mélanges liquides-solides

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DE102005040014A1 (de) * 2005-08-23 2007-03-01 Putzmeister Ag Vorrichtung zum Fördern von Dickstoffmaterial
DE102014108236A1 (de) * 2014-06-12 2015-12-17 Gea Mechanical Equipment Gmbh Vollmantel-Schneckenzentrifuge und Verfahren zu deren Betrieb
EP3814708B1 (fr) * 2018-06-28 2023-04-19 GEA Process Engineering A/S Séchoir et procédé de séchage d'une charge liquide en une poudre
RU2716354C1 (ru) * 2019-09-16 2020-03-11 Общество с ограниченной ответственностью Научно-производственная фирма "Теплоэнергопром" Сушильное устройство с псевдоожиженным слоем
RU196301U1 (ru) * 2019-12-20 2020-02-25 Федеральное государственное бюджетное образовательное учреждение высшего образования "Волгоградский государственный технический университет" (ВолгГТУ) Распылительная сушилка для жидких материалов

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CN101726160B (zh) * 2009-11-10 2013-04-17 中国烟草总公司郑州烟草研究院 一种分散物料气流干燥装置
RU2607445C1 (ru) * 2015-12-14 2017-01-10 Олег Савельевич Кочетов Гранулятор кипящего слоя
RU2647003C1 (ru) * 2017-06-29 2018-03-13 Олег Савельевич Кочетов Сушилка для растворов и суспензий
RU2647921C1 (ru) * 2017-06-29 2018-03-21 Олег Савельевич Кочетов Распылительная сушилка со встречными закрученными потоками типа взп
EP3737900A4 (fr) * 2018-01-16 2022-03-16 Waister AS Système modulaire et procédé de séchage de solides et de mélanges liquides-solides
CN113070154A (zh) * 2021-03-09 2021-07-06 上饶中材机械有限公司 一种高效除尘的水泥熟料输送机
CN113070154B (zh) * 2021-03-09 2023-04-25 上饶中材机械有限公司 一种高效除尘的水泥熟料输送机

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AU2003302692A1 (en) 2004-06-23
DE10256674A1 (de) 2004-06-17
AU2003302692A8 (en) 2004-06-23

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