US3667131A - Fluid energy drying mill - Google Patents

Fluid energy drying mill Download PDF

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Publication number
US3667131A
US3667131A US44152A US3667131DA US3667131A US 3667131 A US3667131 A US 3667131A US 44152 A US44152 A US 44152A US 3667131D A US3667131D A US 3667131DA US 3667131 A US3667131 A US 3667131A
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inlet chamber
gaseous fluid
mill
slurry
inlet
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US44152A
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English (en)
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Nicholas N Stephanoff
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Fluid Energy Processing and Equipment Co
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Fluid Energy Processing and Equipment Co
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • B01D1/18—Evaporating by spraying to obtain dry solids
    • 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
    • F26B17/101—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 the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis
    • F26B17/105—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 the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis the shaft or duct, e.g. its axis, being other than straight, i.e. curved, zig-zag, closed-loop, spiral

Definitions

  • FLUID ENERGY DRYING NIILL [72] Inventor: Nicholas N. Stephanofl, Haverford, Pa.
  • ABSTRACT A fluid energy drying mill wherein the material to be dried is a liquid slurry of solid particles or of solids in solution.
  • the slurry, upon being fed into the mill is immediately atomized and flash-dried, the atomization being accomplished by high pressure, high velocity gaseous fluid jets, while the flash-drying is effected by very hot, low pressure, gaseous fluid jets.
  • the hot gaseous fluid jets comprise a plurality of gaseous fluid streams which enter from at least four difi'erent sides surrounding the feed inlet and converge at a focal point downstream of the inlet whereby the hot gaseous fluid both encompasses the fed material and concentrates its heat energy in the path of the fed material.
  • the flash-dried particles are then centrifugally passed through the curved portion of the mill and centrifugally exhausted from the mill during their passage.
  • bypass ducts may be provided between the downstack portion of the mill and the inlet chamber where atomization and flashdrying takes place whereby vapors from the downstack are used to break any vacuum in the inlet chamber and may also be used as a tempering means to avoid case hardening of the particles.
  • SHEET 20E 2 ATTOR EY FLUID ENERGY DRYING MILL
  • This invention relates to a fluid energy drying mill, and it particularly relates to a drying mill for liquid slurries and the like.
  • Fluid energy drying mills have heretofore been used and have proven generally satisfactory for their intended purposes. Mills of this type utilize the system of atomization of the particles in the slurry and very rapid or flash-drying of the particles before they have an opportunity to agglomerate.
  • the dried particles are then passed through a centrifu gally accelerated curved path during which the most completely dried (i.e., the lightest) particles are carried around on the inner periphery of the centrifugal stream while the less completely dried (i.e., the heavier) particles are positioned on the outer periphery of the stream.
  • the lighter particles on the inner periphery pass through an exhaust duct positioned adjacent the inner periphery, while the heavier particles pass back into the drying area to be mixed with additional raw material for further drying.
  • Another object of the present invention is to provide a fluid energy drying mill where vacuum conditions at the feed inlet are avoided and where inadvertent case hardening of the particles is obviated without interfering with the total flash-drying effect.
  • FIG. 1 is a sectional view of a mill embodying the present invention.
  • FIG. 2 is a sectional view taken on line 22 of FIG. 1.
  • FIG. 3 is a fragmentary top plan view of the mill of FIG. 1.
  • FIG. 4 is a fragmentary side elevational view of a modified form of the mill of FIG. 1.
  • FIG. 5 is a sectional view taken on line 5-5 of FIG. 4.
  • FIG. 6 is an enlarged elevational view of a modified form of feed assembly.
  • FIG. 1 a drying mill, generally designated 10, comprising a relatively straight inlet chamber 12 merging into an arcuate elbow section 14 which forms the lower end of an upstack 16.
  • the upstack 16 is connected by an elbow section 18 to a section 20 which includes an elbow section 22 connecting it to a downstack 24.
  • an exhaust duct 26 lead ing to a collection station (not shown) or to a dust collector (not shown), or to another treating section, all of which form no part of the present invention, in and of themselves.
  • a manifold 28 supplied with hot low pressure gaseous fluid such as air, steam, or the like, and which may be as high as 3,000 F. or even higher, from a source (not shown), is provided with a plurality of nozzles 30, 32 and 34 which direct such heated gaseous fluid into the inlet 12 at varying angles whereby the fluid streams converge toward the upstack 16.
  • a similar nozzle is provided at 36, and the fluid stream from nozzle 36 also converges with the other streams.
  • the fluid stream from nozzle 36 converges with a stream of hot, low pressure gaseous fluid from a noale 38 which is connected to a standpipe 40 leading from the manifold 28.
  • the intersection of fluid streams from nozzles 36 and 38 takes place at a point designated 42 at the front portion of the inlet chamber 12 just below the downstack 24.
  • angularly directed streams of hot, low pressure gaseous fluid from lateral nozzles 44 and 46 (see FIG. 3) which are also connected to the standpipe 40.
  • a conical hot fluid shield substantially envelops the atomized slurry particles as they are propelled linearly into the inlet chamber so that all the particles are subjected to the heat of the fluid streams.
  • the four converging hot fluid streams focus their combined heat energy at one focal area. This results in increased heat energy and a far greater flash-drying effect than if only the hot gaseous fluid from the nozzles 30, 32 and 34 were used, especially since the latter rapidly dissipate some of their heat energy.
  • the fluids from the nozzles 30, 32 and 34 aided by that from the nozzle 36, which is also used for flash-drying, not only provide the primary centrifugal force, but the heat thereof also serves to prevent too rapid a cooling of the flash-dried particles during their centrifugally actuated passage through the mill.
  • the inlet chamber 12 is closed by a front plate 48 (best seen in FIG. 2) which is connected to a peripheral flange of the open front end of the chamber by means of screws, bolts, or the like indicated at 50.
  • the noules 44 and 46 are attached to this plate, as indicated in FIG. 2.
  • Also mounted in this plate are a pair of parallel high pressure nozzles 52 and 54 connected to a source of high pressure gaseous fluid (not shown), by a flexible or adjustable connection.
  • These nozzles 52 and 54 are preferably axially adjustable into the chamber 12. Such adjustment may be accomplished by any desirable means. As illustrated herein, the adjustment is accomplished by permitting the nozzles to move axially through corresponding apertures in the plate and then holding them in fixed adjusted position by means of pins or the like indicated at 56 and 58 respectively.
  • Each high pressure nozzle 52 and 54 is associated with a slurry feed nozzle, as at 60 and 62 respectively.
  • the nozzles 60 and 62 are connected to a source of slurry (not shown) by a flexible or adjustable connection.
  • the nozzles 60 and 62 each have an upwardly extending outlet portion (as shown in FIG. 1) which is positioned adjacent the outlet of the corresponding high pressure nozzle 52 or 54. 7
  • Each feed nozzle 60 and 62 is axially adjustable in the same manner as the nozzles 52 and 54. They are held in adjusted positions by pins or the like indicated at 64 and 66. They are also provided with keys, as at 68 and 70 to prevent rotation.
  • the slurry is propelled, under low pressure, from the feed nozzles 60 and 62 in an upward direction.
  • the slurry issues from the feed nozzles, it is entrained in the jet of high pressure, high velocity gaseous fluid issuing from the corresponding nozzle 52 or 54.
  • the high pressure, high velocity fluid immediately atomizes the slurry and propels it forwardly into the inlet chamber 12.
  • the atomized material is propelled forwardly, it is acted upon by the very hot gaseous fluid from the nozzles 36, 38, 44 and 46 which cause instaneous flashddrying of the atomized particles.
  • high pressure nozzles 72 and 74 connected to a source of high pressure gaseous fluid (not shown) by flexible or otherwise adjustable connections. These nozzles 72 and 74 are also axially adjustable similarly to nozzles 52 and 54 and nozzles 60 and 62, and are shown held in adjusted positions by pins or the like 76 and 78.
  • FIGS. 4 and 5 there is shown a modified form of the mill shown in FIGS. 1, 2, and 3.
  • This modification takes advantage of the aforementioned characteristic of the mill whereby the return to the inlet chamber is substantially free of solid particles.
  • the return comprises, in efiect, only the gaseous fluid used as the centrifugal conveying means. A portion of this fluid is by-passed into the inlet chamber and breaks any vacuum which tends to form therein as a result of the high velocities of the atomization nozzles and as a result of the sudden reduction of space-filling material due to the atomization and flash-drying.
  • the apparatus for accomplishing this vacuum breaking is shown in H08. 4 and 5 and comprises a pair of ducts, designated 100 and 102 7 extending angularly from the downstack 104, similar to downstack 24, into the inlet chamber 106, similar to inlet chamber 12. As seen in FIG. 5, the ducts 100 and 102 have laterally ofiset lower portions which extend into opposite sides of the inlet chamber. As the gaseous fluid passes transversely into the inlet chamber 106 from opposite sides thereof, the gaseous fluid envelops the entire area and quickly breaks any vacuum. Since there are little if any solid particles in the by-passed gaseous fluid, there is no possibility of their clogging the area.
  • this fluid which is still hot but which has lost some of its heat during the centrifugal motion, acts to somewhat temper the very hot gases causing the flash-drying, thereby permittingthe use of even higher temperatures than would otherwise be feasible.
  • these gases are extremely hot, they may cause case hardening of the particles whereby a hard skin is formed on the outside before the inside is completely dried. This is especially applicable to those processes where solids in solution are being treated.
  • the bypassed fluid is just cool enough to prevent such case hardening but is not cool enough to seriously interfere with the flash-drying. In fact, it causes just enough instantaneous delay in the drying to permit thorough drying before case hardening occurs.
  • calcium stearate which melts at 300 F. may be dried, utilizing the present invention, at from 650 to 750 F.
  • the end product has a temperature of only about to F.
  • the material being dried may be of any composition.
  • it may be a solution, either aqueous or utilizing any other diluent.
  • It may be an aqueous slurry of precipitated iron oxide or of white or yellow silica.
  • it may be a slurry of solid particles in any other liquid diluent such as isoproponal, methanol, perchloroethylene, trichloroethylene, etc.
  • the present mill is well adapted to aid in the deodorization of the finished products.
  • the flash-drying process also causes vaporization of the liquids.
  • FIG. 6 shows a modified form of feed means wherein the parts are essentially the same as those shown at 52, 54, 60, 62, 72 and 74 in FIG. 1, except that the feed nozzle 200 is provided with a cooling jacket 202.
  • the jacket 202 is connected to a source of cooling fluid (not shown) by a hose or the like (not shown).
  • the fluid may be either liquid, such as cold water, etc., or gaseous, such as air, Freon gas, etc. This aids in the prevention of crusting of the feed line.
  • a drying mill comprising an inlet chamber having a front end and a rear end, a generally arcuate tubular portion extending from the rear end of said inlet chamber and having an exhaust duct intermediate thereof and a return section connected to said inlet chamber adjacent the front end thereof, at least one conveyor nozzle entering said inlet chamber at an angle tangential to the longitudinal axis of said inlet chamber, said conveyor nozzle being connected to a source of hot, low pressure gaseous fluid, a feed inlet at the front end of said inlet chamber, said feed inlet being connected to a source of solids containing slurry, atomizing means in said inlet chamber for atomizing the slurry issuing from said feed inlet, said atomizing means comprising an atomizing nozzle connected to a source of high pressure gaseous fluid, and a plurality of enveloping nozzles positioned radially outward of said inlet nozzle and atomizing means and inclined toward each other, said enveloping nozzles being connected to a source of hot, low
  • a drying mill comprising an inlet chamber having a front end and a rear end, a generally arcuate tubular portion extending from the rear end of said inlet chamber and having an exhaust duct intermediate thereof and a return section connected to said inlet chamber adjacent the front end thereof, at least one conveyor nozzle entering said inlet chamber at an angle tangential to the longitudinal axis of said inlet chamber,
  • said conveyor nozzle being connected to a source of hot, low pressure gaseous fluid, a feed inlet at the front end of said inlet chamber, said feed inlet being connected to a source of solids containing slurry, atomizing means in said inlet chamber for atomizing the slurry issuing from said feed inlet, and a plurality of enveloping nozzles positioned radially outward of said inlet nozzle and atomizing means and inclined toward each other whereby'they act to direct intersecting streams of hot, low pressure gaseous fluid within said inlet chamber toward a focal point intermediate the front and rear ends of said inlet chamber and rearwardly of said feed inlet and atomizing means, said enveloping nozzles being connected to a source of hot, low pressure gaseous fluid, and at least one by-pass duct connected between said return section and said inlet chamber at a position adjacent said feed inlet and atomizing means.
  • a method of drying particles in a slurry which comprises passing the slurry into the inlet chamber of a generally arcuate mill, atomizing the slurry as it enters said inlet chamber, enveloping the atomized particles with angularly directed streams of hot gaseous fluid while directing said hot gaseous fluid toward a focal point rearwardly of the entering slurry and while propelling the atomized particles toward said focal point, centrifugally propelling the resultant particles around an arcuate path and through an exhaust duct positioned in said arcuate path, and by-passing gaseous fluid from said arcuate path into a position adjacent the entering slurry as it is atomized.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Drying Of Solid Materials (AREA)
US44152A 1970-06-08 1970-06-08 Fluid energy drying mill Expired - Lifetime US3667131A (en)

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Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3814316A (en) * 1973-06-18 1974-06-04 Fluid Energy Process Equip Dryer feed nozzle assembly
US3945130A (en) * 1975-01-10 1976-03-23 Fluid Energy Processing & Equipment Co. Expanded chamber centrifugal drying mill
US3974574A (en) * 1975-03-10 1976-08-17 Fluid Energy Processing & Equipment Co. Centrifugal drying mill
US4033853A (en) * 1976-01-16 1977-07-05 Great Canadian Oil Sands Limited Process and apparatus for heating and deaerating raw bituminous froth
US4098006A (en) * 1977-03-08 1978-07-04 Uop Inc. Organic waste dewatering and drying process
US4121349A (en) * 1977-07-07 1978-10-24 Uop Inc. Organic waste drying process
US4161825A (en) * 1977-03-08 1979-07-24 Uop Inc. Plasticized organic waste
US4489503A (en) * 1980-11-28 1984-12-25 Olin Corporation Process for drying wet particles of available halogen compounds
US5181987A (en) * 1990-06-13 1993-01-26 Bunkawerke Huls Gmbh Device and process for precipitating polymers
US5266211A (en) * 1990-06-13 1993-11-30 Bunawerke Huls Gmbh Process for precipitating polymers
US20030141028A1 (en) * 2001-10-30 2003-07-31 Weyerhaeuser Company Dried singulated cellulose pulp fibers
US20030188838A1 (en) * 2001-10-30 2003-10-09 Yancey Michael J. Process for producing dried singulated crosslinked cellulose pulp fibers
US6769199B2 (en) 2001-10-30 2004-08-03 Weyerhaeuser Company Process for producing dried singulated cellulose pulp fibers using a jet drier and injected steam and the product resulting therefrom
US6782637B2 (en) 2001-10-30 2004-08-31 Weyerhaeuser Company System for making dried singulated crosslinked cellulose pulp fibers
US6862819B2 (en) 2001-10-30 2005-03-08 Weyerhaeuser Company System for producing dried singulated cellulose pulp fibers using a jet drier and injected steam
US20050086828A1 (en) * 2001-10-30 2005-04-28 Weyerhaeuser Company Process for producing dried, singulated fibers using steam and heated air
US20060101665A1 (en) * 2004-07-19 2006-05-18 Christianne Carin Process and system for drying and heat treating materials
US20060254081A1 (en) * 2004-07-19 2006-11-16 Earthrenew, Inc. Process and system for drying and heat treating materials
US20090165974A1 (en) * 2007-12-28 2009-07-02 Weyerhaeuser Co. Methods for blending dried cellulose fibers
US7610692B2 (en) 2006-01-18 2009-11-03 Earthrenew, Inc. Systems for prevention of HAP emissions and for efficient drying/dehydration processes
US7617617B2 (en) 2004-07-19 2009-11-17 Earthrenew, Inc. Process and apparatus for manufacture of fertilizer products from manure and sewage
US7694523B2 (en) 2004-07-19 2010-04-13 Earthrenew, Inc. Control system for gas turbine in material treatment unit
US20230053323A1 (en) * 2021-08-02 2023-02-16 Canon Kabushiki Kaisha Flash drying apparatus and method of producing particles

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107166911A (zh) * 2017-05-11 2017-09-15 无锡科技职业学院 一种气流式干燥器

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2297726A (en) * 1938-04-02 1942-10-06 Thermo Plastics Corp Method and apparatus for drying or the like
US3339286A (en) * 1965-03-11 1967-09-05 Fluid Energy Proc And Equipmen Method and apparatus for drying wet pulverulent material in a gaseous path
US3403451A (en) * 1965-03-30 1968-10-01 Fluid Energy Proc & Equipment Method for drying or treating wet solid and semisolid materials

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2297726A (en) * 1938-04-02 1942-10-06 Thermo Plastics Corp Method and apparatus for drying or the like
US3339286A (en) * 1965-03-11 1967-09-05 Fluid Energy Proc And Equipmen Method and apparatus for drying wet pulverulent material in a gaseous path
US3403451A (en) * 1965-03-30 1968-10-01 Fluid Energy Proc & Equipment Method for drying or treating wet solid and semisolid materials

Cited By (44)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3814316A (en) * 1973-06-18 1974-06-04 Fluid Energy Process Equip Dryer feed nozzle assembly
US3945130A (en) * 1975-01-10 1976-03-23 Fluid Energy Processing & Equipment Co. Expanded chamber centrifugal drying mill
US3974574A (en) * 1975-03-10 1976-08-17 Fluid Energy Processing & Equipment Co. Centrifugal drying mill
US4033853A (en) * 1976-01-16 1977-07-05 Great Canadian Oil Sands Limited Process and apparatus for heating and deaerating raw bituminous froth
US4098006A (en) * 1977-03-08 1978-07-04 Uop Inc. Organic waste dewatering and drying process
US4099336A (en) * 1977-03-08 1978-07-11 Uop Inc. Organic waste drying process
US4128946A (en) * 1977-03-08 1978-12-12 Uop Inc. Organic waste drying process
US4161825A (en) * 1977-03-08 1979-07-24 Uop Inc. Plasticized organic waste
US4121349A (en) * 1977-07-07 1978-10-24 Uop Inc. Organic waste drying process
US4489503A (en) * 1980-11-28 1984-12-25 Olin Corporation Process for drying wet particles of available halogen compounds
US5181987A (en) * 1990-06-13 1993-01-26 Bunkawerke Huls Gmbh Device and process for precipitating polymers
US5266211A (en) * 1990-06-13 1993-11-30 Bunawerke Huls Gmbh Process for precipitating polymers
US6910285B2 (en) 2001-10-30 2005-06-28 Weyerhaeuser Company Process to produce dried singulated cellulose pulp fibers
US20080010853A1 (en) * 2001-10-30 2008-01-17 Weyerhaeuser Co. Process for Producing Dried Singulated Fibers Using Steam and Heated Air
US6748671B1 (en) 2001-10-30 2004-06-15 Weyerhaeuser Company Process to produce dried singulated cellulose pulp fibers
US20040123483A1 (en) * 2001-10-30 2004-07-01 Vrbanac Michael David Process to produce dried singulated cellulose pulp fibers
US6769199B2 (en) 2001-10-30 2004-08-03 Weyerhaeuser Company Process for producing dried singulated cellulose pulp fibers using a jet drier and injected steam and the product resulting therefrom
US6782637B2 (en) 2001-10-30 2004-08-31 Weyerhaeuser Company System for making dried singulated crosslinked cellulose pulp fibers
US20040177936A1 (en) * 2001-10-30 2004-09-16 Vrbanac Michael David Dried singulated cellulose pulp fibers
US6862819B2 (en) 2001-10-30 2005-03-08 Weyerhaeuser Company System for producing dried singulated cellulose pulp fibers using a jet drier and injected steam
US6865822B2 (en) 2001-10-30 2005-03-15 Weyerhaeuser Company Drying system for producing dried singulated cellulose pulp fibers
US20050086828A1 (en) * 2001-10-30 2005-04-28 Weyerhaeuser Company Process for producing dried, singulated fibers using steam and heated air
US20030141028A1 (en) * 2001-10-30 2003-07-31 Weyerhaeuser Company Dried singulated cellulose pulp fibers
US7018508B2 (en) 2001-10-30 2006-03-28 Weyerhaeuser Company Process for producing dried singulated crosslinked cellulose pulp fibers
US7334347B2 (en) 2001-10-30 2008-02-26 Weyerhaeuser Company Process for producing dried, singulated fibers using steam and heated air
US20030188838A1 (en) * 2001-10-30 2003-10-09 Yancey Michael J. Process for producing dried singulated crosslinked cellulose pulp fibers
US7290353B2 (en) 2001-10-30 2007-11-06 Weyerhaeuser Company System for making dried singulated crosslinked cellulose pulp fibers
US8407911B2 (en) 2004-07-19 2013-04-02 Earthrenew, Inc. Process and system for drying and heat treating materials
US20060101665A1 (en) * 2004-07-19 2006-05-18 Christianne Carin Process and system for drying and heat treating materials
US7487601B2 (en) 2004-07-19 2009-02-10 Earthrenew, Inc. Process and system for drying and heat treating materials
US10094616B2 (en) 2004-07-19 2018-10-09 2292055 Ontario Inc. Process and system for drying and heat treating materials
US20060254081A1 (en) * 2004-07-19 2006-11-16 Earthrenew, Inc. Process and system for drying and heat treating materials
US7617617B2 (en) 2004-07-19 2009-11-17 Earthrenew, Inc. Process and apparatus for manufacture of fertilizer products from manure and sewage
US7685737B2 (en) * 2004-07-19 2010-03-30 Earthrenew, Inc. Process and system for drying and heat treating materials
US7694523B2 (en) 2004-07-19 2010-04-13 Earthrenew, Inc. Control system for gas turbine in material treatment unit
US7866060B2 (en) 2004-07-19 2011-01-11 Earthrenew, Inc. Process and system for drying and heat treating materials
US7882646B2 (en) 2004-07-19 2011-02-08 Earthrenew, Inc. Process and system for drying and heat treating materials
US7966741B2 (en) 2004-07-19 2011-06-28 Earthrenew, Inc. Process and apparatus for manufacture of fertilizer products from manure and sewage
US7975398B2 (en) 2004-07-19 2011-07-12 Earthrenew, Inc. Process and system for drying and heat treating materials
US7610692B2 (en) 2006-01-18 2009-11-03 Earthrenew, Inc. Systems for prevention of HAP emissions and for efficient drying/dehydration processes
US8156662B2 (en) 2006-01-18 2012-04-17 Earthrenew, Inc. Systems for prevention of HAP emissions and for efficient drying/dehydration processes
US20090165974A1 (en) * 2007-12-28 2009-07-02 Weyerhaeuser Co. Methods for blending dried cellulose fibers
US20230053323A1 (en) * 2021-08-02 2023-02-16 Canon Kabushiki Kaisha Flash drying apparatus and method of producing particles
US12358186B2 (en) * 2021-08-02 2025-07-15 Canon Kabushiki Kaisha Flash drying apparatus and method of producing particles

Also Published As

Publication number Publication date
DE2041036A1 (de) 1971-12-16
ES381631A1 (es) 1973-04-16
FR2186842A5 (2) 1974-01-11

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