US3807705A - Process and apparatus for solids blending - Google Patents

Process and apparatus for solids blending Download PDF

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Publication number
US3807705A
US3807705A US00267200A US26720072A US3807705A US 3807705 A US3807705 A US 3807705A US 00267200 A US00267200 A US 00267200A US 26720072 A US26720072 A US 26720072A US 3807705 A US3807705 A US 3807705A
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Prior art keywords
solids
bed
blending
weight fractions
residence time
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English (en)
Inventor
R Humkey
D Marshall
D Ryan
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EIDP Inc
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EI Du Pont de Nemours and Co
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Priority to US00267200A priority Critical patent/US3807705A/en
Priority to CA173,108A priority patent/CA982550A/en
Priority to GB2932473A priority patent/GB1435995A/en
Priority to JP7135073A priority patent/JPS5316932B2/ja
Priority to NLAANVRAGE7308969,A priority patent/NL183386B/xx
Priority to IT25915/73A priority patent/IT990718B/it
Priority to DE2332948A priority patent/DE2332948C2/de
Priority to FR7323665A priority patent/FR2190504B1/fr
Application granted granted Critical
Publication of US3807705A publication Critical patent/US3807705A/en
Assigned to CHASE MANHATTAN BANK, THE reassignment CHASE MANHATTAN BANK, THE SECURITY INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: CAIN CHEMICAL INC., A CORP. OF DE.
Assigned to CAIN CHEMICAL INC., A DE CORP. reassignment CAIN CHEMICAL INC., A DE CORP. RELEASED BY SECURED PARTY (SEE DOCUMENT FOR DETAILS). RECORDED JUNE 8, 1987, AT REEL 4722, FRAME 520-526. Assignors: CHASE MAHATTAN BANK (NATION ASSOCIATION, THE, AS AGENT
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/40—Mixers using gas or liquid agitation, e.g. with air supply tubes
    • B01F33/405—Mixers using gas or liquid agitation, e.g. with air supply tubes in receptacles having guiding conduits therein, e.g. for feeding the gas to the bottom of the receptacle
    • B01F33/4051—Mixers using gas or liquid agitation, e.g. with air supply tubes in receptacles having guiding conduits therein, e.g. for feeding the gas to the bottom of the receptacle with vertical conduits through which the material is being moved upwardly driven by the fluid
    • B01F33/40511—Mixers using gas or liquid agitation, e.g. with air supply tubes in receptacles having guiding conduits therein, e.g. for feeding the gas to the bottom of the receptacle with vertical conduits through which the material is being moved upwardly driven by the fluid with a central conduit or a central set of conduits

Definitions

  • ABSIRACI A process and apparatus for the blending of a bed of particulate solids operating cyclically by selectively 2% 259/95 regulated downward gravity flow of a fraction of the i 95 96 solids, fluidized mixing outside of the bed, followed by l 1 0 are bid recycle to the top of the bed.
  • this invention comprises a process for blending a bed of particulate solids comprising, in sequence, maintaining different residence times of separate weight fractions of the solids within the bed while withdrawing the solids in downward gravity flow from the bed, feeding the weight fractions of solids to a common gas fluidization mixing zone, intimately mixing the solids by gas fluidization and recycling the solids from the mixing zone to the bed, together with apparatus for conducting the process.
  • FIG. 3 is a partially schematic cross-sectional side el- 4 evation view of a second embodiment of blender according to this invention provided with helical baffles,
  • FIG. 4 is a partially schematic cross-sectional side elevation view of a third embodiment of blender according to this invention provided with both planar baffles and an enlarged antechamber at the inlet end of the draft tube,
  • FIG. 5 is a partially schematic cross-sectional side elevation view of a solids flow throttling means for a fourth particularly preferred embodiment of this invention.
  • FIG. 5A is an enlarged (2X) view looking upwards from line 5A-5A, FIG. 5,
  • FIG. 6 is a log-log plot of Mixer Weight Fraction versus Number of Displacements to Blend for the two conditions (a) layer flll and (b) 0.5'fill for apparatus according to this invention
  • FIG. 7 is a plot of Residence Time Ratio (Maximum/- Minimum) versus Number of Displacements to Blend as to which the Mixer Weight Fraction (1) was preselected to be 0.05, 0.10 and 0.20, respectively,
  • FIG. 8 is a plot of Residence Time Ratio (Maximum/- Minimum) versus Number of Displacements to Blend wherein the Column Residence Time was preselected to increase linearly with column number for Mixer Weight Fractions (f) of 0.02, 0.05 and 0.10, respectively,
  • FIG. 9 is a plot of Residence Time Ratio (Maximum/- Minimum) versus Number of Displacements to Blend, with Mixer Weight Fraction (f) 0.10 in all cases for the different total number of columns of solids exiting the apparatus preselected to be 3, 4, 5, 6 and I2, respectively, 1
  • FIG. 10 is a plot of Residence Time Ratio (Maximum/Minimum) versus Number of Displacements to Blend for two different two column-blenders operating with 0.5 fill and having preselected Mixer Weight Fractions (1) of 0.1 and 0.2, respectively,
  • FIGS. 11A and 11B are plots of Number of Displacements versus Marker Concentration in Exit for two column apparatus configurations operating with 0.2 Mixer Weight Fractions for an in-phase Residence Time Ratio (Maximum/Minimum) of 2.1 and an out-of-phase Residence Time Ratio (Maximum/Minimum) of 1.6, respectively,
  • FIG. 12 is a schematic side elevation crosssectional view of a 4-column physical model apparatus which was constructed to verify the mathematically predicted operation of blending apparatus constructed according to this invention
  • FIG. 13 is a comparative plot of Residence Time Ratio (Maximum/Minimum) versus Number of Displacements to Blend (0) as computed and (b) as measured using the apparatus of FIG. 12,
  • FIG. 14 is a plot of Column Number versus Column Displacement Time/Blender Displacement Time for the conditions (a) column residence time linear with column number (full line plot) and (b) column velocity linear with column number (broken line plot), respectively,
  • FIG. 15 is a broken section plan view looking upwards of a preferred design of solids flow-constricting valves employed in a preferred embodiment of this invention.
  • FIG. 16 is a sectional view taken on line l616, FIG. 15.
  • Solids blending according to this invention is intended to have application to quite uniformly sized particulate solids, such as pelletized polyethylene and the like, as distinguished from solids mixtures having a relatively wide distribution of particle sizes such as, for example, dry Portland cement-aggregate mixes.
  • This invention utilizes sequential l. gravity-flow downward progression of solids through a relatively dense bed, during which a substantial proportion of the solids are delayed in passage-by baffles or other flow regulators whereas the remainder of the solids gravitates downwardly relatively unhindered,
  • one embodiment of our apparatus comprises a vessel having a cylindrical top section 1 1 closed at the bottom by a frusto-conical bottom section 12.
  • a draft tube 15 is, in this design, mounted coaxially of top section 11 with lower end in open communication with bottom section 12 and upper end in open communication with top section 11.
  • Optimum solids loading level for the apparatus is along line aa, disposed slightly below the top end of tube 15.
  • the roof closure of the apparatus which is not critical to operation, in this instance consists of a squat frus to-conical member 16 which is provided with a centrally located gas discharge pipe 17 and a raw unblended solids introduction pipe 18 in circuit with which is valve 19.
  • a solids deflector 20 is disposed coaxially with respect to tube 15 about one tube radius thereabove and provided with a circularly dished, downwardly oriented deflection hood 20a. Solids striking hood 20a are deflected downwardly into the main bed of solids, de-
  • Conical bottom section 12 is provided with a plenum chamber 24 extending around the entire circumference of the cone at about half height, the bottom edge of which is sloped downwardly to provide, with the inner wall overhang 121; of the cone, a continuous peripheral slot 25 through which solids fluidizing gas is supplied via nozzles 26 spaced at equal angular intervals around the cone section outside periphery.
  • a T-fitting 28 is connected to the apex of conical section 12 with the axial branch fitted with a solids gravityflow drain valve 28a.
  • the side branch, 28b is a nozzle for the supply of entrainment gas during solids blending operation of the apparatus.
  • main entrainment gas supply nozzle 29 is inserted through the side wall of cone 12 with discharge end aligned axially upward of draft tube 15 at a level approximately one draft tube diameter below the lower end of tube 15, giving particularly good solids entrainment.
  • nozzle 29 comprises an upwardly bent pressurized air supply conduit 29a provided at its discharge end with an upwardly directed conically-formed hollow check valve element 42, which is raised axially upward from its seat at the discharge end 29b of conduit 29a to permit air discharge upwardly from nozzle 29.
  • the valve is provided with an axially disposed threaded guide shaft 43 which is secured against rotation at its upper end within the hollow base member 42a of valve element 42 by pin 44 inserted through drilled hole 45 aligned with a companion blind bore 46 disposed diametrically opposite thereto.
  • Pin 44 lies loosely across a transverse flat 47 formed by cutting away approximately one half of the thickness of the upper end of shaft 43.
  • the lower end of shaft 43 is slidably guided within a vertical tube piece 48 coaxially supported by an open spider horizontal framework 49 weld-attached to'the inside of conduit 29a.
  • a set screw SO-attached to the base end is slidable within longitudinal slot 50a cut in piece 48, thereby locking shaft 43 against rotation during screw adjustment of valve element 42 longitudinally of shaft 43.
  • the blender of FIG. 1 is provided with four planar baffles at the same horizontal level supported by struts 30a connecting with the inside wall of section 11 and the exterior of draft tube 15.
  • Baffles 30 are disposed equiangularly around the annular blender inner space at approximately equal end spacings of, typically, 6.5 percent of the diameter of section 11 from confronting apparatus elements and at inward inclinations of, typically, 34 with respect to the vertical.
  • the upper ends'of baffles 30 lie at, typically, 10 percent bed depth level below a-a, with the lower ends at about percent total bed depth level.
  • the collective projected areas of baffles 30 aggregate about percent of the full annular cross-sectional area bounded by the inside periphery of top section 11 and the outside periphery of draft tube 15.
  • a second set of four planar baffles 31, not shown in full in FIG. 1, identical in all respects with baffles 30, is mounted coparallel with and in vertical alignment with respect to baffles 30 at a typical spacing therefrom of approximately 10 percent of bed depth.
  • the upper ends of baffles 31 thus lie at about 55 percent bed depth, whereas the lower ends lie at about 90 percent bed depth.
  • start-up is preferably effected by first introducing the solids to be blended and then supplying fluidizing gas, usually air, unless a different gas is required for chemical activity reasons, via nozzles 26.
  • fluidizing gas usually air
  • the fluidizing gas pressure is preselected in relationship to bed 23 depth so that the bed seals against excessive gas leakage, a pressure drop of, typically, 2 inches H O/ft. of bed depth being taken in the blending of high density polyethylene having a roughly spherical particle size of 2.5 to 3.5 mm. in diameter.
  • valve 290 and the gas supply valve (not shown) connected with side branch 28b are opened to introduce enough entrainment gas to elevate solids from the bottom of section 12, whereupon a fluidized solids zone extending over substantially the full depth of cone l2, i.e., below line bb, for typically, to percent of the diameter of the cylindrical section, is maintained below the lower end of draft tube 15, with some solids entrainment through tube 15 occurring.
  • a fluidized solids zone extending over substantially the full depth of cone l2, i.e., below line bb, for typically, to percent of the diameter of the cylindrical section, is maintained below the lower end of draft tube 15, with some solids entrainment through tube 15 occurring.
  • nozzle 29 can be adjustable in elevation for further control of solids entrainment. Solids flow in lbs/min. can be adjusted over a broad range, as detailed in the report of
  • the particles in bed 23 are supported in air to an extent where they possess a low angle of repose of about 18.
  • the particles overlying baffles 30 and 31 are delayed somewhat as compared to the downward progress of the remaining particles.
  • different residence times of separate weight fractions of the solids within the bed 23 are maintained while withdrawing the solids in downward gravity flow from the bed, which effects blending during progress of the solids through the bed.
  • Vigorous blending next ensues within the fluidization zone of conical section 12, followed by yet more blending during solids entrainment recycle through tube 15.
  • FIG.. 3 there is shown a second embodiment of blending apparatus employing a pair of identical twin flight, half turn helical plate baffles 33 and 34 mounted coaxially with respect to central draft tube 15'.
  • These baffles have a radius, referred to the longitudinal axis of the blender apparatus such that the outer limit lineof the baffles lies at approximately 60 percent of the bed 23' radial extent.
  • Upper baffle 33 occupies approximately the first quarter of bed 23' depth, whereas lower baffle 34 occupies approximately the last quarter.
  • Helical baffling has proved especially effective for high ratio length-to-dianieter blender configurations. All remaining construction is as hereinbefore described for the blender of FIG. 1.
  • FIG. 4 there is shown a design of blender wherein the draft tube 15" is expanded at the lower end to provide an ante-chamber 37 having its lower end completely within frusto-conical bottom secment and thus realizes economies.
  • the antechamber can conveniently comprise 5 blended was particulate polyethylene in the general two frusto-conical elements 37a and 37b joined by size range of 2.5 to 3.5 mm. diameter.
  • the inlet opening 38 to antechamber 37 is approximately the same diameter as the inside diameter of tube 15", and the converging walls of frusto-conical element 37b diverge slightly away from the confronting walls of frusto-conical bottom section 12" after approaching to the closest clearance corresponding to about 90 percent of the radius of the vessel cone at the junction line of element 37a with element 37b.
  • Angle a of antechamber 37 measured, typically, 113, so that the wall 37a is sloped away from the horizontal at an angle of about 57, much greater than the angle of repose of about 27 for the polyethylene pellets being blended. The foregoing angles apply for vessels having conical sections 12" of 60 included angle.
  • the annular area measured at the level of the juncture line of elements 37a and 37b should be in the range of about 5-2O percent of the full horizontal section area of cylindrical shell 11'', dependent on the diameter and height of draft tube 15". This is done to dccrease the bed air flow necessary to obtain the AP for conveying in the draft tube.
  • the AP/ft. in the annular area must not exceed about 6 inches H O/ft., otherwise one does not get downward pellet flow.
  • FIG. 4 is otherwise similar in all respects to the design hereinbefore described with reference to FIG. 1, except that only four planar baffles 30" instead of eight are required due to its lower height.
  • Operation of the apparatus of FIG. 4 is the same as described for the other embodiments, except that, due to the placement nozzle 29" within opening 38, fluidization of the solids processed occurs largely within antechamber 37 and, as to it, within the side angle regions almost exclusively.-The central path is taken by entrained particles, as indicated by the smaller number particle density represented within this space.
  • Example I An important advantage of the antechamber construction described is that much more stable fluidization is obtained, because of removal of the weight of the higher pellets in the bed.
  • the added resistance presented to gas leakage out through annular passage 40 reduces markedly the operating gas require-
  • Example I the blending apparatus of FIG. 3 was operated without baffles 33 and 34 installed; however, blending was conducted with sequential fluidization in the conical bottom section followed by draft tube entrainment, pellet and air separation and gravity flow through the packed bed, and uniform blended product was obtained after 35 minutes of operation with the gas (in this instance air) and pellet flow reported.
  • This Example shows that relatively long blending times tend to be required for vessels having a large overall height diameter ratio.
  • Example II shows that the blending time for the same material processed in the same height/diameter ratio blender using the same air flow rate, but with the apparatus provided with helical baffles 33 and 34 as shown in FIG. 3, can be dramatically reduced to 5 minutes.
  • Example III shows the increase in air consumption required as the diameter of the blending vessel is increased. With eight planar baffles and the high pellet flow rate of 260 lbs/min. reported,blending time was reduced to the very low value of 2.5 minutes, but at the cost of a considerably increased air flow rate.
  • Example IV In an effort to reduce air consumption, the identical apparatus of Example III was altered for Example IV by disposing the lower end of draft tube 15 well below, i.e., 12 inches below, the knuckle line, whereupon air consumption was reduced by at least 35 percent. However, the blending time increased approximately in the same proportion to 3.5 minutes.
  • Example V illustrates the advantage of the antechamber in reducing air consumption, the apparatus of FIG. 4 realizing a blend time change over the unbaffled apparatus of Example I about in the same proportion to the increase in air consumption. As compared with the apparatus of Example IV, the'apparatus of Example V also shows enhanced efficiency.
  • apparatus of this invention performs an incidental classification action during blending operation, in that fines are entrained out of discharge pipe 17 and can be readily recovered in a downstream air filter. This can be a concurrent benefit accompanying the blending, especially where the solids are ultimately used as extrusion stock where particle size uniformity is essential for long term extrusion machine set-up adjustments and the like.
  • FIGS. and 5A Another design of apparatus utilizing an expanded antechamber 37' is that detailed in FIGS. and 5A, in which the upper cylindrical shell 11" is omitted for simplicity in the showing.
  • baffles 30 and 31 are omitted and an arcuate solids flow restricter plate 53, sloped outwardly an amount of about 30 at the top edge to prevent hang-up of solids and attached around the lower end of element 37b, is substituted.
  • Plate 53 overlies the solids escape end of frusto-conical section 12" and thereby throttles flow of solids therethrough to preserve a preselected differential flow throughout the annular space surrounding draft tube 15".
  • baffles 54 For best results in the prevention of solids cross-flow, it is preferred to mount vertical baffles 54 around the entire circumference of the annular volume defined by element 37b and the inside surface of cone bottom 12". A typical number of ten such baffles is shown in FIG. 5A, in this instance disposed circumferentially at equiangular spacings of 36 apart, although, if desired, a different circumferential distribution can be employed in order to obtain yet other individual solids weight fraction flows as hereinafter described.
  • the profile of plate 53 was chosen to preserve a so]- ids residence time, by which is meant the time a particle dwells in bed 23, varying linearly with the number of individual solids delivery channels defined by baffles 54, starting from 9 oclock position and going to 3 oclock position, as seen in FIG. 5A. Since the plate is symmetrical about the 3 oclock-9 oclock axis, apertures in mirror image relationship on opposite sides of this axis deliver equal weight fractions of solids, so that the term different residence times, as employed in the claims, is not limited to the situation where the residence time of each separate solids weight fraction delivered from the bed 23 is, in fact, different from all others delivered from the bed.
  • MVF Mixer Weight Fraction
  • f the proportion of solids maintained in a highly agitated and fluidized state
  • RTR Residence Time Ratio
  • an average circulation time i.e., the average time to move the top of the bed to exit and return
  • RTR Residence Time Ratio
  • RTD Residence Time Distribution
  • FIGS. 6-10 and FIGS. 11A and 11B illustrate some of the results of blending experiments conducted on a computer with the mathematical model.
  • FIG. 6 is a log-log plot of Mixer Weight Fraction versus Number of Displacements (turnovers through blending apparatus) to Blend (NDB)
  • RTR Residence Time Ratio
  • FIG. 7 (for a 100 equal weight fraction, i.e., column, apparatus) is a linear plot of the Number of Displacements to Blend (NDB) versus the Residence Time Ratio (RTR) with parameters of M WF (Mixer Weight Fraction).
  • NDB Number of Displacements to Blend
  • RTR Residence Time Ratio
  • M WF Mater Weight Fraction
  • FIG. 8 is again a plot of the NDB (Number of Displacements to Blend) versus Residence Time Ratio with parameters of Mixer Weight Fraction.
  • RTD Residence Time Distribution
  • the residence time (rather than velocity) for each weight fraction was increased linearly with weight fraction number while maintaining the ratio of the slowest to the fastest as shown.
  • FIGS. 7 and 8 a surprising reduction in turnovers to blend from 3.2 (FIG. 7) to about 2.] (FIG. 8) for a 0.05 Mixer was obtained with this manner of adjusting Residence Time. Note also that the optimum RTR was about 4.0 for a 0.05 fraction Mixer.
  • FIG. 9 is a plot of the NDB against the RTR with parameters of the number of equal weight fractions withdrawn from the blending system.
  • the well-mixed volume contains 0.1 of the total weight of pellets and the residence time is distributed linearly with weight fraction number. Layer fill was used in this test to determine the number of weight fractions required.
  • the plot shows that increasing the number of equal weight fractions withdrawn from 3 to 6 reduces the NDB and decreases the sensitivity to Residence Time Ratio (RTR). Further increasing the number of equal weight fractions withdrawn from 12 to was found to make almost no change in the NDB. Comparing FIGS. 8 and 9 permits another comparison of the increased time to blend (approximately one additional displacement) when testing with a thin layer of markers on top of the bed.
  • FIG. 10 relates the NDB versus the RTR for a simple two equal weight fraction model with the well-mixed fractions of 0.1 and 0.2. Note the wide oscillation in NDB as the RTR is increased from I to 3 and note that two minima are obtained.
  • concentration of markers exiting the mixer by which is meant the concentration of black, blue or other distinctively colored minority particles incorporated astrace material
  • FIG. 11A for the RTR (2.1) coinciding with a maximum NDB.
  • FIG. 118 indicates the marker concentration vs. number of displacements (time) for the RTR (1.6) coinciding with a minimum NDB.
  • the mathematical model is basically very straightforward, and the only assumption required is that the solids can be made to flow in the manner described.
  • FIG. 12 to further substantiate its validity, a four-column physical model was built and tested. Separate conveying lines were used such that adjusting the air flow permitted adjusting the Residence Time in each column. Separate inlet pipes were used to assure maximum uniformity of residence time in each column. The conveyors empty into a separating vessel and the impingement created a region of high pellet velocity and a great deal of random movement Measurements indicated that about 2 percent of the total pellets were in this well-mixed zone at any given time.
  • FIG. l4 is included to better describe the concepts of Residence Time Ratio (RTR) and Residence Time Distribution (RTD).
  • RTR Residence Time Ratio
  • RTD Residence Time Distribution
  • FIG. 14 the Column Residence Time divided by the Blender Displacement Time is plotted against the column number.
  • the column residence time is that required for a pellet within said column to travel from the top of the column and return to its-starting position, since no mixer was used. All pellets within a single column have been given the same residence time and, in the example illustrated, eight columns are used to make up the blender. Thus each column represents one-eighth of the total weight to be blended.
  • the blender displacement time was found by dividing the blenderweight by the sum of the flow from each column. This sum, or the total recirculation flow,
  • FIGS. 15 and 16 The design of FIGS. 15 and 16 is shown as having only four solids flow control valves, although, of course, a greater number is preferred and can be readily accommodated without interference one with another.
  • the individual valves 56 conveniently constitute cutout sections of an inwardly nested false conical bottom section telescoped within conical bottom section 12", each section being hinge-supported at the upper ends 56a to permit lateral movement with respect to element 37b.
  • Push rods 57 are provided for preselected settings of each individual valve.
  • valves 56 In order to close off the interspaces between adjacent edges of valves 56, pyramidal filler blocks 58, rigidly supported against movement by secure attachment at their outboard faces to the stationary skirt section 12", are mounted between valve pairs. Then, as valves 56 open or close, the edges thereof slide over the pyramidal sides of blocks 58 close enough thereto to bar escape of any solids particles being blended but with sufficient clearance to avoid frictional binding of the moving valve edges with respect to the tiller blocks.
  • the inboard edges of pyramidal blocks 58 can extend inwardly far enough to constitute partially effective separators barring any circumferential displacement of solids from one column to another.
  • Full length baffling equivalent to that hereinbefore described with reference to FIGS. 5 and 5A can then be achieved by welding fins 54' to the inboard edges of the pyramidal blocks as shown in FIG. 16, in which case the inner edges abut at all times against the confronting outside surface of element 37b (omitted from this view to better show the details of the filler blocks).
  • Residence Time Ratio should be controlled between about 1.5 and 5.0, depending on the mixer size, number of columns, composition difference to be blended, and the Residence Time Distribution.
  • An RTR smaller than 1.5 invariably cause excessive concentration amplitude peaks as the material exits the mixer, and thus longer blend times.
  • An RTR larger than 5.0 causes longer blend times due to the time required to displace the slower moving columns. There is not a direct relationship between RTR and blend times, but the optimums'lie within the 1.5-5.0 range.
  • Residence Time Distribution and the number of columns employed should be designed to obtain the most constant feed of the concentration disturbance into the mixer and therefore the smallest amplitude of concentration cycles exiting the mixer. Thus, a residence time distribution that is linear with column numher and a larger number of columns are desirable.
  • the number of columns should preferably be more than five for most blending tasks.
  • the method of blending a bed of particulate solids comprising, in sequence, maintaining different residence times of separate weight fractions of said solids within said bed while withdrawing said solids in downward gravity flow from said bed, feeding said weight fractions of solids to a common gas fluidization mixing zone, intimately mixing said solids by gas fluidization, and recycling said solids from said mixing zone to said bed.
  • Apparatus for blending a bed of particulate solids comprising, in combination, a vessel containing said bed of particulate solids, gas fluidization solids mixing means, means maintaining different residence times of separate weight fractions of said solids within said bed while withdrawing said solids in downward gravity flow from said bed and delivering said solids to said gas fluidization mixing means, and solids recycling means delivering said solids in intimately mixed condition from said gas fluidization solids mixing means back to said bed.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mixers With Rotating Receptacles And Mixers With Vibration Mechanisms (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
US00267200A 1972-06-28 1972-06-28 Process and apparatus for solids blending Expired - Lifetime US3807705A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US00267200A US3807705A (en) 1972-06-28 1972-06-28 Process and apparatus for solids blending
CA173,108A CA982550A (en) 1972-06-28 1973-06-04 Solids blending process combining a layering by gravity flow with mixing by fluidization and apparatus
GB2932473A GB1435995A (en) 1972-06-28 1973-06-20 Process and apparatus for solids blending
JP7135073A JPS5316932B2 (enrdf_load_stackoverflow) 1972-06-28 1973-06-26
NLAANVRAGE7308969,A NL183386B (nl) 1972-06-28 1973-06-27 Inrichting voor het mengen van korrelig materiaal.
IT25915/73A IT990718B (it) 1972-06-28 1973-06-27 Processo ed apparecchio per il mescolamento di solidi
DE2332948A DE2332948C2 (de) 1972-06-28 1973-06-28 Verfahren und Vorrichtung zum Mischen von teilchenförmigen Feststoffen
FR7323665A FR2190504B1 (enrdf_load_stackoverflow) 1972-06-28 1973-06-28

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JP (1) JPS5316932B2 (enrdf_load_stackoverflow)
CA (1) CA982550A (enrdf_load_stackoverflow)
DE (1) DE2332948C2 (enrdf_load_stackoverflow)
FR (1) FR2190504B1 (enrdf_load_stackoverflow)
GB (1) GB1435995A (enrdf_load_stackoverflow)
IT (1) IT990718B (enrdf_load_stackoverflow)
NL (1) NL183386B (enrdf_load_stackoverflow)

Cited By (18)

* Cited by examiner, † Cited by third party
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US3953003A (en) * 1974-06-06 1976-04-27 Aluterv Aluminiumipari Tervezo Vallalat Tank provided with pneumatic mixing pipe
US4037825A (en) * 1975-04-14 1977-07-26 Herwig Burgert Loop reactor for chemical processes
US4097927A (en) * 1975-08-02 1978-06-27 Chimkombinat Apparatus for mixing bulk materials
US4151932A (en) * 1977-04-20 1979-05-01 Wachtler Frank A Distribution tower for particulate material
US4172667A (en) * 1977-06-06 1979-10-30 General Electric Company Method and apparatus for blending powders in a fluidized bed
US4185926A (en) * 1978-02-28 1980-01-29 Westinghouse Electric Corp. Safe-geometry pneumatic nuclear fuel powder blender
US4194444A (en) * 1975-11-05 1980-03-25 Smitherm Industries, Inc. Particulate solids
US4246836A (en) * 1975-11-05 1981-01-27 Smitherm Industries, Inc. Apparatus for processing particulate solids
US4569596A (en) * 1985-11-26 1986-02-11 Fuller Company Pneumatic conveying and material blending apparatus and method
US4740087A (en) * 1986-12-16 1988-04-26 Illinois Tool Works Inc. Magnetic particle bath suspension apparatus
US4834544A (en) * 1987-07-06 1989-05-30 Fuller Company Fines separation system for pellet blender
US5644971A (en) * 1995-06-13 1997-07-08 Andritz Sprout-Bauer, Inc. Vessel for steeping of grain
US20050260043A1 (en) * 2002-08-31 2005-11-24 Lange Neville E Fluidising apparatus
CN102335977A (zh) * 2011-06-02 2012-02-01 张毅 植物纤维与热塑性塑料复合粒料的生产方法及设备
WO2015199547A1 (en) * 2014-06-24 2015-12-30 Kca Deutag Drilling Norge As Drilling fluid sheargun
US20160346745A1 (en) * 2015-05-27 2016-12-01 The Young Industries, Inc. System for mixing/blending fine bulk materials
RU2703311C1 (ru) * 2019-04-15 2019-10-16 Федеральное государственное бюджетное образовательное учреждение высшего образования "Донской государственный аграрный университет" (ФГБОУ ВО Донской ГАУ) Бункерное устройство для обрушения сводов сыпучего материала
US12318741B2 (en) 2019-02-05 2025-06-03 Jagtech As Method and device for conditioning drilling fluid

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CA1211142A (en) * 1984-04-04 1986-09-09 Robert E. Romanchik Pneumatic conveying and material blending apparatus and method
DE3430633A1 (de) * 1984-08-20 1986-02-27 Herbert 7853 Steinen Hüttlin Fliessbettapparatur
DE3838500A1 (de) * 1988-11-12 1990-05-23 Budapesti Porcelangyar Verfahren und vorrichtung zur hydromechanischen verarbeitung von in wasser dispergierbaren mineralstoffen
RU2596184C1 (ru) * 2015-03-30 2016-08-27 Федеральное государственное бюджетное образовательное учреждение высшего образования "Южно-Уральский государственный аграрный университет" (ФГБОУ ВО Южно-Уральский ГАУ) Устройство для транспортирования и смешивания сыпучих материалов

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US3647188A (en) * 1970-03-25 1972-03-07 Fuller Co Airlift blending apparatus

Cited By (21)

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Publication number Priority date Publication date Assignee Title
US3953003A (en) * 1974-06-06 1976-04-27 Aluterv Aluminiumipari Tervezo Vallalat Tank provided with pneumatic mixing pipe
US4037825A (en) * 1975-04-14 1977-07-26 Herwig Burgert Loop reactor for chemical processes
US4097927A (en) * 1975-08-02 1978-06-27 Chimkombinat Apparatus for mixing bulk materials
US4194444A (en) * 1975-11-05 1980-03-25 Smitherm Industries, Inc. Particulate solids
US4246836A (en) * 1975-11-05 1981-01-27 Smitherm Industries, Inc. Apparatus for processing particulate solids
US4151932A (en) * 1977-04-20 1979-05-01 Wachtler Frank A Distribution tower for particulate material
US4172667A (en) * 1977-06-06 1979-10-30 General Electric Company Method and apparatus for blending powders in a fluidized bed
US4185926A (en) * 1978-02-28 1980-01-29 Westinghouse Electric Corp. Safe-geometry pneumatic nuclear fuel powder blender
US4569596A (en) * 1985-11-26 1986-02-11 Fuller Company Pneumatic conveying and material blending apparatus and method
US4740087A (en) * 1986-12-16 1988-04-26 Illinois Tool Works Inc. Magnetic particle bath suspension apparatus
US4834544A (en) * 1987-07-06 1989-05-30 Fuller Company Fines separation system for pellet blender
US5644971A (en) * 1995-06-13 1997-07-08 Andritz Sprout-Bauer, Inc. Vessel for steeping of grain
US20050260043A1 (en) * 2002-08-31 2005-11-24 Lange Neville E Fluidising apparatus
US7364347B2 (en) * 2002-08-31 2008-04-29 Axsia Serck Baker Limited Fluidising apparatus
CN102335977A (zh) * 2011-06-02 2012-02-01 张毅 植物纤维与热塑性塑料复合粒料的生产方法及设备
CN102335977B (zh) * 2011-06-02 2013-06-19 张毅 植物纤维与热塑性塑料复合粒料的生产方法及设备
WO2015199547A1 (en) * 2014-06-24 2015-12-30 Kca Deutag Drilling Norge As Drilling fluid sheargun
US20160346745A1 (en) * 2015-05-27 2016-12-01 The Young Industries, Inc. System for mixing/blending fine bulk materials
US9833755B2 (en) * 2015-05-27 2017-12-05 The Young Industries, Inc. System for mixing/blending fine bulk materials
US12318741B2 (en) 2019-02-05 2025-06-03 Jagtech As Method and device for conditioning drilling fluid
RU2703311C1 (ru) * 2019-04-15 2019-10-16 Федеральное государственное бюджетное образовательное учреждение высшего образования "Донской государственный аграрный университет" (ФГБОУ ВО Донской ГАУ) Бункерное устройство для обрушения сводов сыпучего материала

Also Published As

Publication number Publication date
NL183386B (nl) 1988-05-16
GB1435995A (en) 1976-05-19
JPS4964061A (enrdf_load_stackoverflow) 1974-06-21
FR2190504A1 (enrdf_load_stackoverflow) 1974-02-01
FR2190504B1 (enrdf_load_stackoverflow) 1978-02-17
NL7308969A (enrdf_load_stackoverflow) 1974-01-02
CA982550A (en) 1976-01-27
DE2332948A1 (de) 1974-01-10
DE2332948C2 (de) 1987-02-12
JPS5316932B2 (enrdf_load_stackoverflow) 1978-06-05
IT990718B (it) 1975-07-10

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