• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A pulverulent, water soluble material is agglomerated by projecting the material in a stream through a moistening zone, directing steam or mist towards the stream in the moistening zone so that the stream is surrounded by steam or mist flowing inwardly towards the stream, thereby moistening and fusing the particles, and then drying the material. Particles of the material may be engaged with one another to form chunks before moistening.
    公开号:SU1723997A3
    申请号:SU864027810
    申请日:1986-07-01
    公开日:1992-03-30
    发明作者:Хсу Шенг-Хесунг
    申请人:Сосьете Де Продюи Нестле С.А. (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method of agglomerating water-soluble powdered materials and a device for its implementation.
    The aim of the invention is to improve the quality of the material obtained.
    The method of agglomeration of a water-soluble powdered material involves moistening the powdered material by feeding it through the moistening zone from top to bottom, and water gas is supplied through a circular section horizontally from the periphery around the entire circumference of the chamber towards the flow axis of the powdered material and subsequent drying, wherein
    Simultaneously with the supply of the powder material and in the same direction, water gas is supplied along the periphery of the material flow at a subsonic speed. In addition, it is possible to additionally introduce a cooling gas in the direction of flow of the powdered material along its periphery, and the cooling gas can be fed into the flow of powdered material after the moistening zone.
    In the proposed methods, the powdered material is introduced into the stream through a humidification zone. The water gas directs the flow from the periphery of the flow so that the water flowing to the center of the flow surrounds the flow. The term water gas
    N5 SO Yu
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    with
    as used in the description, implies water vapor and aerosols from small droplets of pods dispersed in water vapor or in another gas. Water gas wets the particles, forming a liquid or quasi-liquid phase on the surfaces of the particles. Collapsing or contiguous particles are interconnected by fusing the corresponding liquid or quasi-liquid phases, thereby forming agglomerates. The latter are then dried to solidify the fused phases and crushed to particles of the desired size.
    Inwardly flowing water gas tends to limit the flow of powdered material within a relatively small volume, thereby maximizing the number of particles per unit volume or density of particles in the stream. The relatively high particle density prevailing in the flow increases the likelihood of contact between the particles in the wetting zone and, consequently, increases the likelihood of fusion between the particles. The inward-flowing water gas has a relatively low velocity and does not create significant turbulence. Under relatively immobile conditions prevailing in the wet zone, the particles are in contact with each other at low relative speeds, further increasing the likelihood of fusion. Preferably, at least most of the water gas is introduced into the humidification zone with a zero velocity component in a direction parallel to the direction of movement of the particles. Due to the fact that water gas does not noticeably accelerate particles in their path, the residence time of the particles in the humidification zone is maximized, additionally contributing to the fusion of the particles.
    The conditions of the process in the moistening operation can be selected either to thoroughly wet all particles in each lump and, consequently, to achieve an effect of uniform darkening, or to thoroughly wet the particles on the outer surfaces of the lumps, but not to fully moisten the particles inside the lumps. Such uneven wetting leads to the formation of agglomerates dark in appearance and light inside. Upon subsequent grinding, the bright inner areas are emptied and form bright grains, similar to roasted ground coffee.
    Preserving the lump structure during wetting contributes to the preservation of odor. Particle odor loss
    inside each piece is minimized due to the protective effect of the surrounding particles.
    Proposed methods of agglomeration
    allow adjustment of the product structure — particle shape, color, and density — to provide essentially any desired combination of these properties within extremely wide limits. So
    Thus, instant coffee can be agglomerated to produce either sharp-edged granules resembling roasted and ground coffee, or spongy particles that resemble ordinary agglomerated products of any color from tan to dark brown, bordering black, and any bulk density from about 17 r / dl to about 30 g / dl.
    In addition, if water vapor is used as a water gas, the sintering processes of the material take place at lower rates of water vapor injection compared to the steam jet processes used before. Such low rates of water vapor help minimize the loss of volatile and aromatic components of the material.
    The particle size of the processed material has a significant effect on the results achieved. Particles less than about 50 microns in size facilitate the formation of lumps before moistening. Handling such small particles
    using the proposed methods using a preliminary operation for the formation of lumps or without using it helps to obtain an agglomerated product with an acute angle
    granular structure. Larger particles up to 200 microns in size tend to form a tubular structure. With even larger particle sizes, the degree of agglomeration decreases markedly.
    Very large particles can be processed in accordance with the proposed methods in order to ensure their darkening without appreciable sintering.
    The invention also provides
    an improved device for processing powdered material,
    The apparatus may include means for feeding the material stream in the direction of flow, means for supplying water gas such that water gas passing inwards in the direction of flow surrounds the stream, and means for drying the material. The device may also include means for combining the particles among themselves with
    the formation of lumps and means for grinding the material after it is moistened, o
    FIG. 1 schematically shows the proposed device option; Fig, 2 - the same, a partial section, an enlarged scale; in fig. 3 - the device, the second option; in fig. 4 - the same, axonometric, third option; in fig. 5 is the fourth option.
    The device (Fig. 1) includes a feeder hopper 1 connected via a pneumatic conveying system 2 and a heat exchanger 3 with a spray gun 4, which in turn is connected to a loading device 5. The latter comprises a tubular body 6 provided with an opening 7 at its output end and a screw screw 8 rotatably mounted inside the housing. The screw 8 is connected to the variable speed motor 9.
    Hole 7 is connected to the inlet of the feed hopper 10 of the fitting 11 assembly, the heads of which are mounted on the top of the dryer 12. The fitting 11 in the assembly includes a feeding pipe 13 connected to the bottom of the feeding hopper 10, while the inlet includes an annular feed hole 14 on its bottom or output end. The top of the feed hopper 10 communicates with the atmosphere.
    Coaxially the inlet nozzle has several rings of fitting 15 so that the rings of the nozzle surround the lower end of the inlet nozzle and extend slightly below the supply hole 14. The inner ring of the nozzle and the wall of the inlet nozzle jointly form an annular gap communicated with the atmosphere. The fitting rings together form a pair of annular steam openings 16, which are connected to a source of water 17 by means of a pressure regulator valve 18. Other necessary devices (not shown) may also be provided to record and control the flow rate, pressure and temperature of the water vapor supplied to the holes, and to remove condensate from the water vapor.
    The node 19 of the diffuser 20 is installed under the rings of the nozzle and the inlet. The assembly 19 comprises a porous cylindrical housing or a flange of baked stainless steel that is coaxial with respect to the supply pipe 13, and this flange limits the humidification chamber 21 under the inlet.
    The casing has a wide number of micropores made in it, while the pores are evenly distributed over the surface
    casing. The structural wall 22 defines an annular channel 23 surrounding the casing and located opposite the outer surface of the casing around its outer circumference. The annular channel is connected 5 by means of an adjustable control valve 24 to the source 17 of water vapor and for adjusting the vapor conditions inside the annular channel 23 and removing condensate from the water vapor
    0, additional recording and adjusting devices are provided (not shown). The top cover 25 connects the structural wall 22 with the outer ring of the fitting 15 so that the upper or output end
    5, the humidification chamber 21 is closed, with the exception of the outlet, annular gap and steam openings.
    Directly under the constructive wall 22 is installed aspirator
    0 ring 26. The annular gap in the aspirator ring is connected to a narrow inward and downward annular nozzle 27 adjacent to the lower or output end of the diffuser 20, and this annular
    5 pipe coaxial with respect to the casing. The slit 28 is connected by means of the control regulator 29 to the source 30 of compressed air.
    Fitting assembly 11 mounted on top
    0 and 12 is located on the same axis with a hole in the lid of the chamber, while there is a gap 31 between the outer surface of the fitting and the edges of the hole. The dryer can be the chamber of a conventional dryer, known as the top entry dryer. Such a dryer includes appropriate conventional equipment (not shown) connected to a chamber for heating air and feeding
    0 heated air through the chamber. Air control equipment is provided to maintain a slight vacuum inside the chamber. Holes 32 for product exit (Fig. 1) are provided near the bottom of the chamber. The dust collector is installed to trap small particles from the air leaving the chamber and to return the collected particles back to the pneumatic transport system 2.
    0 An opening 32 for product to exit the drying chamber is connected to a sifter device or classifier 34 installed to separate the incoming material by size. In the classifier
    5 34 there is an outlet 35 for loading particles of large sizes, an opening 36 for discharging small particles and an opening 37 for transporting material with a desired average particle size. A device such as a fluidized bed contactor can be connected with an outlet for cooling the discharged product. nym layer (not shown). The opening 36 for unloading small particles is connected to the pneumatic conveying system 2. An aperture 35 for unloading large particles is connected via a lifting conveyor 38 to a grinder 39, which in turn is set to return material to the input of the classifier 34.
    The chopper 39 may include a pair of opposing parallel shafts, each of which has a plurality of disc-shaped toothed blades so that the blades on each shaft / 1 are located between the blades on the opposite shaft. For a rapid rotation of the shafts, an appropriate drive (not shown) is provided so that the material entering the chopper 39 passes between the blades on the opposite shafts.
    According to one of the methods, the particles formed as a result of spray-drying an aqueous extract of roasted coffee are passed from the feeder bin 1 through the heat exchanger 3 to the atomizer 4. The smallest particles are sent from the grinder to the charging device 5. The screw 8 is rotated by the electric motor 9 in order to feed the particles down through the hole 7,
    The material passes down from the hole 7 through the feed hopper 10 into the feed tube 13 of the fitting 11 of the assembly (FIG. 2) and falls through the feed hole 14 to the bottom of the tube. Thus, the flow of the crushed material with a generally circular cross section, the diameter of which is approximately equal to the diameter of the supply opening 14, is directed from the supply opening downwards or in the direction of flow mainly in the vertical section along the longitudinal axis 40 of the supply pipe. The water source 17 and the regulator valve 24 maintain in the annular channel 23 a predetermined pressure of water vapor. The water vapor diffuses through the casing wall of the diffuser 20 and flows inward in the direction of the longitudinal axis 40, forming a cloud in the humidification chamber 21. When particles come into contact with water vapor, part of the water vapor condenses on the particles.
    Since the annular channel 23 does not have appreciable resistance to the flow of water vapor and is opposite the casing of the diffuser 20 along its entire circumference, the casing of the diffuser is subjected to equal pressure of water vapor along its entire perimeter. Since the casing has an almost uniform porosity, water vapor
    diffuses through the casing with practically
    at the same speed throughout their ne. meter and enters humidification chamber 21 with
    at the same, low speed in the radial direction along the longitudinal axis 40. Water vapor passing through the casing outflows the casing surface in a direction perpendicular to the casing surface and,
    0 therefore has essentially zero speed in a vertical direction parallel to the axis.
    Steam supplied to annular openings 16 under very low pressure.
    5 with the help of the pressure regulating valve 18 passes downward from the orifices at a subsonic speed in the immediate vicinity of the flow particles and mixes with the cloud, supplying additional water
    0 for wetting the particles.
    Steam coming out of the steam holes prevents the cloud from spreading upwards and also carries the downward flow relative to
    5 cold ambient air through the annular gap and through the open top of the feed hopper 10 and the feed pipe 13. The air cools the inlet and prevents the entry of water vapor into the inlet
    0 pipe. This, in turn, prevents sticking of the material in the inlet to its walls. As cold air flows down into the vapor cloud, it contributes to the condensation of water vapor.
    5 on the surface of the particles.
    The compressed air passes from the annular gap 28 into the aspirator ring (exhaust fan) through the annular nozzle 27 and moves down or along with a significant
    0 at a speed parallel to the longitudinal axis 40. Since air is released at the same speed around the axis, the air does not tend to deflect particles in the direction perpendicular to the axis. Descending
    5, the downward flow of air from the annular nozzle is encountered with particles and gases in the vicinity of the lower edge of chamber 21 and carries them down into the chamber of dryer 12.
    As the particles pass down through the moistening chamber, the moisture condensed on the particles mixes with the solid particles and dissolves them on the surfaces of the particles. At the same time, the heat transferred by the water vapor to the parts increases the temperature of the material. Both of these effects contribute to the formation of a liquid or quasi-liquid fluid phase on the surfaces of the particles. As the particles collide with each other, the fluid phases on the surfaces of the colliding particles
    are mixed together, thereby causing the particles to fuse into agglomerates.
    When the agglomerates enter the chamber of the dryer 12, they collide with a mixture of ambient air entering the chamber of the dryer through the gap 31, and hot, dry air supplied by the air regulation equipment entering the dryer. The agglomerates cause water to drain from the fluid phase, leaving the particles welded to one another within each agglomerate due to the solid material from the fluid phase. The dried agglomerates exit the chamber through the outlet 32 (Fig. 1) and enter the classifier 34. The agglomerates with larger particles are directed through the conveyor 38 to the chopper 39, where they break down into separate parts. These parts are sent back to the classifier 34. The agglomerates and their particles in the required size range pass from the system through the product exit port 37. The agglomerates and their small pieces are returned back to pneumatic transport 2, where they are again involved in the process with fresh raw materials. The fine particles trapped in the dust collector 33 from the air released from the dryer are returned to the pneumatic transport 2 for return to the process.
    The agglomeration process can be modified by connecting part or all of the particles together to form lumps at the preliminary stage, before the material enters the humidification chamber. The formation of lumps is usually not associated with the fusion of particles among themselves, but instead it is based on the natural tendency of the smallest particles to stick together. This trend increases with decreasing particle size. Particles less than 100 microns in size and more preferably less than about 50 microns in size provide the most satisfactory pre-clumping.
    Pre-clumping can be enhanced by compacting and / or moistening the powdered material before it enters the moistening chamber. Thus, the diameter of the tapered opening 7 of the loading device 5 (FIG. 1) and the flow rate of the powdered material can be chosen so that this material is pressed as it passes through the opening.
    Moistening the material to improve clumping is not related to exposure to particles of liquid water or water gas.
    Air with approximately 60-80% relative humidity can be brought into contact with the powdered material in order to control its humidity. Preferably, the particles have a moisture content ranging from about 2 to 8% by weight. When they are clumped, a range of 3.5–4.5% is preferred, and a humidity of 4% is most preferred. Lumps can form without compaction during normal handling and transport operations, especially if the particle size and moisture are good for lumping.
    The lumps obtained before the moistening operation enter the humidification chamber in the stream of powdered material, and are moistened in the chamber with water vapor. The particles that make up each lump are already in contact with each other. When moistening, the fluid fuz is formed in the intervals between the particles in each lump, thereby melting the particles into agglomerates. Lumps can also fuse between themselves, with individual particles and with agglomerates previously formed from individual particles.
    Before fusion, some friction between lumps can also occur. However, the relatively calm conditions prevailing in the humidification chamber tend to minimize such friction. These conditions favoring clumping — small particle size, compaction and wetting — also contribute to the formation of stronger clumps that prevent friction. Preferably, the process conditions are chosen so that at least part of the lumpy structures is preserved, namely, at least some of the particles interconnected into lumps remain connected during the moistening process and, therefore, are interconnected in the form of agglomerates, entering the dryer chamber.
    Regardless of whether lumps are formed or not formed prior to the moistening operation, the appearance and density of the final product varies depending on the degree of moistening achieved during its passage through the cloud of water gas. Greater moisture tends to produce a darker and slightly less dense product. Pre-lumping provides additional control over the appearance of the product. With relatively high moistening, all surfaces of the particles in each lump are wetted and, therefore, the product undergoes a uniform darkening. The limited moistening provides uneven wetting inside each lump, while the surfaces of the particles inside the lumps are wetted to a lesser extent and, therefore, lighter in color than the surfaces outside the lumps. During grinding, light colored particles are formed, resulting in a product with a non-uniform speckled appearance.
    The degree of moisture varies directly depending on the duration of the lumps in the cloud and directly from the humidity of the cloud.
    The humidity of the cloud depends directly on the flow rate of water vapor introduced into the cloud and is controlled mainly by the flow rate of water vapor through the inlet. Preferred is the flow rate of water vapor through the bore or housing up to about 100 kg per minute per square meter of inlet surface, and more preferred are costs in the range of 5 to 50 kg per minute per square meter of inlet surface . Water vapor entering the humidification chamber with such relatively low costs per unit area does not lead to significant turbulence. For instant coffee, the total flow rate through the inlet is usually about 0.9-2.4 kg per minute per liter of the humidification chamber volume, and about 0.25-0.50 kg / kg of the powder material to be processed.
    The duration of exposure depends directly on the length of the passage of particles through the cloud and / hence on the length of the humidification chamber in a direction parallel to their movement. Moisture chambers are 2.5–20 cm long and approximately 5–25 cm in diameter.
    The duration of exposure depends inversely on the component of the velocity of the gases inside the humidification chamber in the lower direction. The lower velocity component, in turn, depends on the combined effect of water vapor and air entering through the steam holes and the annular gap surrounding the inlet.
    Water vapor introduced through the steam holes tends to accelerate the lumps downward, thereby reducing the degree of moisture achieved. Also excessive steam velocities can cause undesirable turbulence and excessive friction of lumps.
    Preferably, water vapor is introduced through the orifices at the minimum speed necessary to prevent the vapor cloud from spreading upward toward the inlet side. Speeds in the order of 10 m / s can be used. Such a low rate, subcritical flow of water vapor can be achieved by supplying water vapor to the holes at a pressure below 9 kPa and more preferably at a pressure below A kPa (excess) in the humidification chamber. Basically,
    5, the pressure in the chamber is close to atmospheric.
    The air flow into the humidification chamber around the suction inlet and in its cross section is the minimum flow necessary to keep the suction inlet cool and dry. A satisfactory air velocity is through the annular gap surrounding the suction inlet of approximately 1 m / s. Usually
    5, the air velocity through the inlet is smaller compared to the air velocity through the annular gap.
    Water vapor passing through the porous diffuser (inlet) or skin does not affect the low velocity component and, therefore, the flow rate of water vapor through the casing can be adjusted without a significant change in the residence time of the particles in the humidification chamber.
    5 By varying the rate of flow of water vapor (flow) through the casing, the concentration of water vapor or the humidity inside the chamber can be adjusted as necessary to moisten the particles to the desired
    0 degrees. The flow of water vapor through the inlet can be changed without reversing any other side of the process. Thus, the water vapor supplied to the inlet does not have
    5 trends in the seizure of air. Whatever the flow rate of water vapor through the inlet, only air entering the humidification chamber will independently enter around the inlet and pass through
    0 him. This is a significant advantage, since excess air can affect the moistening action of the vapor cloud.
    The water vapor entering the humidification chamber through the inlet has a radial velocity component directed inward toward the flow axis. Thus, at least in the vicinity of the periphery of the chamber, there is an internal stream as well as a stream directed downwards.
    A stream of particles flowing out of the inlet is surrounded by water vapor that passes inward in the direction of the center of the stream from its periphery. The internal steam flow tends to restrict the particles and maintain a relatively narrow stream of particles directly around the axis. This restriction separates the particles from the casing and, therefore, prevents the accumulation of solid material on the casing.
    Placing particles into a narrow stream tends to maintain a relatively high number of particles per unit volume of particles or the density of particles in a stream, thereby increasing the likelihood of collisions between particles in the stream and accelerating sintering. If there are lumps formed at the preliminary stage in the flow, the likelihood of collisions between the lumps and the likelihood of collisions between individual particles and lumps also increase, thus aggravating the agglomeration.
    If a product is required that has a granular structure that resembles roasted and ground coffee or resembles the structure of ordinary, dried at low temperatures soluble coffee, the particles used in the process should have an average size of less than about 40 microns. A clear transition takes place in the range of 40-50 microns; with particles with an average size of more than 50 microns, the product tends to form a spongy structure similar to materials subjected to agglomeration using known methods. With particles with an average size of less than 40 microns, the product has a granular structure and, when wetted and dried, agglomerates with a smooth surface are formed, and during the grinding process they are broken into granules with sharp edges. Inwardly flowing water gas promotes the formation of agglomerates with a smooth surface.
    The indicated particle size refers to the average particle size of the material, determined using light scattering techniques using a microTRAC ™ particle size analyzer supplied by Leeds and Norsepp Instrument -General Signal Corporation, or another instrument with similar characteristics. Particles of the desired size are usually obtained by grinding larger particles.
    These process conditions can be adjusted to create many different combinations of product properties. So
    Thus, a dark, low-density product can be obtained using relatively large particles with a low degree of compaction, or without much compaction, and a relatively high degree of moisture. A product of relatively light high-density color can be obtained by combining small particles, clumping with high compaction and low moisture, whereas; while dark, high density product can be obtained with the same particle size and compaction, but with higher moisture. With regard to soluble coffee, the proposed method can produce products similar to commercial low-temperature dried granules or roasted and ground coffee particles, or in the usual way.
    0 agglomerated coffee of any necessary bulk density in the range of 17-30 g / dL. Usually also various products can be obtained without any modification of the device.
    5 In the device shown in FIG. 3, the spray gun 4 is associated with a chute 41. equipped with a porous base 42. The humidified air under pressure supplied by the control unit 43 with air into the chamber 44 under the base 42 is blown upwards through the porous base. The vibratory generator 45 moderately shakes the tray so that the material introduced into it from the spray gun
    5 moves along a porous base. The moving particles meet with humidified air and are also connected to each other to form lumps that pass into the feed hopper 10 and, therefore, through the fitting 11 and the dryer 12 for processing. The conveying and moistening device thus forms lumps without compaction. If the raw materials supplied in the process have an appropriate moisture content, then an adequate transport device can provide an adequate transport device without any wetting equipment. Although to form lumps according to this method,
    0 use vibration, excessive intense vibration can have the opposite result and can cause lumps to shatter. In another embodiment, the wetting and conveying device may be combined with a compacting device. Thus, the humidifying vibrating conveyor shown in FIG. 3 can be installed between the atomizer 4 and the screw-type charging device 5 (FIG. 1).
    These devices and methods can be modified in many different ways. For example, Classification and grinding operations can be eliminated and the product can be removed directly from the outlet of the dryer. The fine particles, after classification (separation), do not require recirculation, but can instead be used in other ways.
    In yet another embodiment, the same dryer can be used simultaneously for both the sintering process and the drying of the liquid material. While the agglomerated material is introduced through the assembly assembly 11 (Fig. 1), small droplets of the liquid material can be introduced into the dryer using a conventional spray drying nozzle 46. Typically, spray dried particles obtained from such a liquid significantly smaller in size than agglomerates. A significant part of the spray-dried particles captures the moving air inside the dryer, is trapped in the dust collector 33 and sent to the pneumatic transport system 2. Other items The spray-dried particles are separated from the dried lumps in the classifier 34 and passed through the outlet 36 back to the conveyor system. Thus, the spray-dried particles are passed through the sprayer 4 during the agglomeration process. In yet another embodiment, a classifier can be set to hold some spray-dried particles with dried lumps in the final product exiting through the outlet 37, resulting in a product consisting of a mixture of particles of different sizes and structures.
    The device includes a circular feed head to obtain a stream of particles of circular cross section and an outlet in the form of a surface of circular rotation about an axis, aligned with the feed head to obtain a radial flow of water gas in the direction of the axis of flow. The combination of a circular flow of particles and a radial flow of gas ensures the optimal restriction of the flow of powdered particles by water vapor flowing inside. However, other forms may also be used.
    The fitting assembly (Fig. 4) contains an inlet port 47 of rectangular cross-section, defining a slit-like outlet 48 of an elongated shape. The curvature of the powdered material is directed downward in the direction of the plane 49. On opposite sides of the outlet, parallel to its longitudinal axis, there is a pair of water vapor collectors 50 elongated along the length, each with a slit-shaped steam nozzle or outlet 51. Water Noah
    0, the steam exiting through these holes passes downward and draws in cold air through a pair of elongated gaps 52 formed between the nozzles and the inlet.
    5, the diffuser includes a pair of long flat porous plates 53 located on opposite sides of the plane 49, and a pair of short porous plates 54, of which the figure shows
    There is only one plate passing between the long plates at their opposite ends. The porous plates together form a rectangular tube surrounding the path of movement of the particles on all sides.
    5 The water vapor exiting through the long plates passes inward in the direction of the wide surfaces of the particle flow, while the water vapor exiting through the short plates flows inward in the direction of the flow boundaries.
    The diffuser does not require microscopic pores or perforations, as indicated. The diffuser may contain discrete, visible perforations. Term
    5, a diffuser means a body having a perforated or porous surface with pores or perforations arranged so tightly that water vapor exits through pores or perforations.
    0 is mixed in close proximity to the housing in an almost continuous (continuous) flow moving in the direction perpendicular to the surface. Diffusers can be made of fine woven
    5 wire mesh.
    Saturated steam is used as water vapor supplied to the humidification chamber. Superheated steam is less preferable because
    0 usually provides a less moisturizing effect. Wet vapor can also be used, which is a mist of the smallest water droplets in a saturated water vapor. May also be
    5, other gases were used that contain fogs from microscopic water jugs dispersed in gases other than water vapor. Mist can be introduced into the humidification chamber with the desired flow pattern by introducing mist into the humidification chamber through the appropriate channel. For example, the device (FIG. 5) includes an annular casing 55 having an axis 56 and a plurality of radially arranged blades 57. A stream of powdered material enters the humidification chamber along axis 56. Mist introduced into the casing in close proximity to its periphery through its inlets 58, passes radially inward in the direction of the axis 56. Thus, the flow of powdered material is surrounded by mist or water gas passing inward in the direction of the axis.
    In accordance with the proposed technology, it is possible to agglomerate other water-soluble powdered materials other than coffee. The term water soluble powdered material refers to a powdered materal that forms a flowable phase when wetted, regardless of whether the flowable phase is a present solution, and regardless of whether the flowable phase includes all the components of the material. Among the materials that can be agglomerated are instant coffee, instant chicory powder, instant beverage powder, milk powder, and cocoa-based blends.
    The device can also be used to darken specified materials, and other hygroscopic pulverized materials without significant agglomeration. Solid, solid granules of material are directed through the inlet fitting of the choke assembly and exposed to a cloud of water vapor, thereby moistening and darkening the outer surface of each granule. The moistened granules are then dried. The granules treated in this way are usually much larger than the smallest particles fused in the sintering process. Therefore, agglomerates obtained in the sintering process can serve as granules.
    The proposed darkening technology uses water vapor or other water vapors that are effective to achieve the desired darkening effect. Water gas, which forms a quiet cloud on the path of the particles, does not impart any perceptible velocity to the granules passing through the cloud. Accordingly, the supply of water gas and, therefore, the moisture content of the cloud can be increased as necessary to provide the required degree of darkening without affecting the dwell time of the granules in the cloud. In contrast, only limited darkening can be achieved using technology that uses only a jet of water vapor from the nozzle. Attempts to enhance the darkening effect by increasing the consumption of water vapor in such a jet become fruitless, the increased consumption of water vapor gives the granules greater speed and, consequently, reduces the residence time of the granules in the water vapor.
    In one embodiment of the invention, the agglomeration process is controlled in order to obtain fused, but relatively light, agglomerates. Some of these agglomerates are then passed through the darkening process, then mixed again with light colored agglomerates to obtain a product with a multi-colored color. The fittings used to agglomerate and darken the product may be in the same drying chamber. Thus, the material leaving the drying chamber will be a mixture of darkened and non-darkened agglomerates. The outlet of the crusher can be connected to the darkening fitting so that only the pieces resulting from the grinding of agglomerates with an increased particle size will be returned through the darkening operation. Since large agglomerates are obtained only during the agglomeration operation, and not during the darkening (blackening) operation, the material returned to the darkening will not include the previously blackened material.
    Example 1. Spray-dried coffee extract powder is pulverized to medium-sized particles - 24 microns, transported in air to a cyclone collector and transferred from a cyclone collector to a screw feeder. The auger pushes the powder through the outlet at a rate of about 0.35 kg per minute per cm2 of the cross section of the outlet. The powder leaves the outlet (head) in the form of a solid stream that breaks down into lumps when it falls into the inlet pipe of the agglomeration choke.
    The fitting assembly is similar to the fitting shown in FIG. 2, but there is no gap between the annular steam holes and the inlet nozzle, so that the inner annular opening for the escape of water vapor directly surrounds the inlet nozzle. Also missing a ring
    exhaust fan. The diffuser is a porous casing with 1 micron pores. Water vapor with a pressure of 750–1500 Pa is introduced through annular apertures to release steam in the amount of 1.28 x 103 - 2.1 x 10 kg per minute per square meter of the area of the outlet aperture. Water vapor with a pressure of about 17 kPa is supplied over the outer surface of the porous casing and it diffuses through it in an amount of about 13.3 kg per minute per square meter of the surface of the diffuser.
    As the water vapor passes through the cloud inside the casing, the lumps turn into agglomerates. The agglomerates enter the initial drying chamber, where warm, dry air meets them and they are partially dried near their surface. The agglomerates exit this chamber into a fluidized bed, where they are further dried to a final moisture content of about 3.2%. The dried agglomerates pass through a sieve provided with an upper sieve with a hole size of 1.68 mm and a lower sieve with a hole size of 595 microns. Large agglomerates are sent to a chopper and then returned to the sieve, while small particles are returned to the nebulizer.
    The product obtained between the upper and lower sieves consists mainly of sharp-edged particles, shaped like particles of roasted and ground coffee. This product has an accepted dark color with light blotches resembling light colored specks in appearance, found in roasted and ground coffee.
    EXAMPLE 2: When the water vapor pressure supplied to the porous casing as in Example 1 is gradually reduced to 7 kPa and the flow of water vapor through the porous casing, respectively, decreases to approximately 6.7 kg per minute per square meter of the diffuser surface. The product becomes gradually brighter and the density of the product gradually decreases, showing results from a gradual decrease in the degree of moisture. When the pressure of water vapor supplied to the porous casing gradually increases to approximately 0.21 kPa, resulting in an increase in the consumption of water vapor through the porous casing to approximately 19 kg per minute per square meter of the diffuser surface, the product becomes gradually darker with an increased with a density and with particles having sharp edges, I will demonstrate
    thereby results in greater moisture.
    Example 3. Spray-dried instant coffee is treated in the same way as in Example 1, except that the powder is ground only to a particle size of about 50 microns. The product has a spongy, uniformly blackened appearance, it does not have
    0 flocculent appearance with sharp-edged particles.
    Example 4. A mixture of chicory extract is dried to a powder form by sawing in a drying tower directly with air at a temperature of a dry thermometer of about 370 ° C. The resulting powder is captured and sprayed to an average particle size of about 40 microns. Pulverized
    0, the powder is fed through a screw type feeder, having a free output, to a vibrating feeder. The powder passes the MS vibratory feeder through the agglomeration nozzle, similar to that shown in
    5 of FIG. 2, back to the same drying chamber that was used in drying the liquid extract, so that both the agglomerates and the sprayed liquid extract are simultaneously dried.
    0 The diffuser is a porous casing with a nominal pore size of 5 microns. Water vapor is fed into the annular outlet holes at a pressure of about 3 kPa and to the porous casing under
    5 pressure of about 37 kPa. Air is supplied through an exhaust fan ring located under the porous casing in an amount of 0.04 m3 / min.
    The mixture of dried agglomerates and powder particles leaving the dryer is directed to a pressing device equipped with an upper sieve with a hole size of 2.38 mm and a lower sieve with a hole size of 707 microns. The pressing device is provided with an internal grinder to grind large agglomerates until they pass through the upper sieve. Small pieces and powder particles from the spray-drying process pass through both sieves and return to the nebulizer. The product between the upper and lower sieves has a flocculent appearance, with particles having sharp edges that look like particles of fried
    5 and ground coffee, a dark color with some light areas, and a bulk density of 25.0 g / dl.
    Example 5. Single granules subjected to drying at negative temperatures of soluble coffee with a size of about
    2 mm is passed into the drying chamber through a fitting similar to that shown in FIG. 2, due to the fact that the exhaust fan ring is removed. Water vapor diffuses inward through the porous casing in an amount of about 2.1 kg per minute per square meter of the diffuser surface. Additional water vapor flows down through the annular inlet openings surrounding the inlet. The granules initially have a light brown color and a bulk density of about 23.2 g / dL. After passing through the nozzle and dryer, the granules have an exceptionally dark brown color corresponding to the blackest particles of the usual roasted coffee powder, and a bulk density of about 25.5 r / dl. The total consumption of water vapor during the darkening operation reaches 0.42 kg of water vapor per 1 kg of the treated granules.
    Example 6. Spray-dried coffee extract powder is pulverized to particles with an average size of 31 microns and passed into the receiving port of the nozzle (head) of sintering through a screw feeder, having a free exit and a vibrating feeder. The powder does not form lumps in a noticeable degree before entering the agglomeration head.
    The head assembly is similar to the head shown in FIG. 2, except that the exhaust fan ring is removed. The diffuser has corrugations with a nominal size of 5 microns. Water vapor under a pressure of about 1 kPa is fed through annular holes for steam to escape surrounding the inlet. In an amount of about 2.0 x 103 kg per minute per square meter of the surface of the outlet, Water vapor of about 33 kPa pressure is fed to the outer surface of the diffuser and it passes through it in the amount of 45 kg per minute per square meter of the surface of the diffuser.
    As the water vapor passes through the cloud, the powder undergoes agglomeration. The agglomerates are dried and then passed through a sieve equipped with an upper sieve with a hole size of 2.38 mm and a lower sieve with a hole size of 707 microns. Large agglomerates are crushed and returned to the sifter device, while the material in the form of small particles is returned to the atomizer. The product obtained between the upper and lower sieves has a flocculent appearance with particles having sharp edges and resembles dried coffee that has been dried at negative temperatures.
    Example (comparative). A procedure similar to example 6 was repeated using the same powder and the same agglomerating head, except that the porous casing was removed. Water vapor was supplied only through annular holes to release water vapor in an amount of 2 , 0 x 103 kg per minute per square meter of the surface of the outlet. Thus, the sintering process does not correspond to the proposed invention.
    The product has a spongy, uniformly darkened appearance to a greater degree than having sharp edges, a flaky appearance obtained in example 6. With the same powder consumption as in example b, the product yield is approximately two times less than the yield,
    0 obtained in example 6, a smaller part of the powder turns into agglomerates in the desired size range as compared with example 6.
    Example 8. Subjected to drying
    5, by spraying, the tea extract is pulverized to particles with an average size of about 40 microns and agglomerated using the same equipment as in Example 6. The speed
    0, the powder feed (flow rate) into the sinter head is approximately 65% of the flow rate used in Example 6. The steam pressure is adjusted to ensure flow rates are about
    5 1.6 x 10 kg per minute per square meter of outlet surface and about 26 kg per minute per square meter of diffuser surface. In other respects, the method is similar to the method used in
    0 example 6. The product has the appearance of flaky particles with sharp edges and a bulk density of 21 g / dL.
    PRI me R 9. A mixture of cocoa powder, sugar, lecithin and seasoning is ground into
    A hammer mill equipped with a perforated exit sieve with a diameter of 3 mm. The ground material has a wide range of particle size distribution and contains both fine particles.
    0 cocoa, and large particles of sugar, having a characteristic light color. The crushed material is sent to the sintering head with a flow rate of approximately 65% of the flow rate used in Example 6. The pressure of water vapor is chosen in order to ensure flow rates on the order of 2, Ex 103 kg per minute per square meter of diffuser surface. The sowing device has an upper C№- then with openings of 1.19 mm in size and not
    has a lower sieve. All material passing through the top sieve is withdrawn from the system as a product. In other respects, the process is similar to the process used in Example 6. The product has a very dark color. Light sugar particles are coated with cocoa, indicating that small cocoa particles were agglomerated together with sugar particles.
    Example 10. The barley grain extract powder subjected to spray-drying is subjected to grinding to particles with an average size of about 35 microns and is introduced through the sintering head having only one annular opening for the steam to escape and not having an annular gap between the opening for the steam and the inlet . There is no noticeable lumping before the moistening operation. In the moistening operation, steam consumption is used in the order of 4.5 x 10 kg per minute per square meter of outlet area and about 15.6 kg per minute per square meter of diffuser surface. The agglomerates obtained during the moistening process are dried and sieved using an upper sieve with a hole size of 2.38 mm and a lower sieve with a hole size of 707 microns. Large pieces are removed to a greater extent than crushed, small pieces are also removed. The product collected between the upper and lower sieves has an appearance with flaky particles having sharp edges.
    Example 11. Low-fat milk powder with an average particle size of about 85 microns, without appreciable pre-lumping, is introduced into an agglomeration head, similar to that shown in FIG. 2, but without the exhaust fan ring, and having an atomizer with 5 micron pores.
    Water vapor is introduced into annular outlet ports at a pressure of about 1.5 kPa and into a porous casing under pressure of about 42 kPa. The agglomerates formed in the head are dried and sieved with the help of an upper sieve with a hole size of 3.36 mm and a lower sieve with a hole size of 707 microns.
    Large agglomerates are returned to the seedbed and crushed in it. while small particles are recovered for reprocessing. The product obtained between the sieves consists of a piece of irregular shape, has a bulk density of 18 g / dl and is easily dispersed in hot water.
    权利要求:
    Claims (5)
    [1]
    1. The method of agglomeration of water-soluble powdered material, including wetting powdered
    of the material by feeding it through the humidification zone in the direction from top to bottom, and the flow of water gas is carried out through a circular cross section horizontally from the periphery around the entire circumference of the chamber
    towards the axis of the flow of powdered material, and subsequent drying, characterized in that, in order to improve the quality of the material obtained, simultaneously with the supply of the powdered material and in the same direction along the periphery of the flow of material, water gas is supplied at a subsonic rate.
    [2]
    2. A method according to claim 1, characterized in that cooling gas is additionally introduced in the direction of flow of the powdered material along its periphery.
    [3]
    3. A device for the agglomeration of a water-soluble powdered material containing a feed pipe with a feed
    a bore feeding the powder material to the supply pipe, a humidification chamber located under the feeding hole forming a humidification zone, a device for supplying water gas to the humidification chamber and the dryer, in order to improve the quality of the material obtained, it is equipped device for the supply of water vapor in the upper part
    a humidification chamber mounted with a gap coaxially on the outside of the supply pipe, and the device for supplying water gas to the humidification chamber is designed as a diffuser.
    [4]
    4, the apparatus according to claim 3, characterized in that it is provided with means for supplying a cooling gas installed in the gap between the supply pipe.
    [5]
    5. The device according to claim 3, wherein it is provided with a ring mounted coaxially with the chamber and below the latter to form a gap, the ring having a nozzle connected to the gap to direct the cooling gas downwards and
    inward to the particles.
    Fy
    FIG. I
    | I'm 4Y
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1723997A3|1992-03-30|Process and unit for sintering water-soluble powdered material
    US4148325A|1979-04-10|Treatment of tobacco
    US5094156A|1992-03-10|Agglomeration apparatus
    US3554760A|1971-01-12|Method of agglomerating food powder
    US3695165A|1972-10-03|Process and apparatus for agglomeration
    US4724620A|1988-02-16|Agglomeration apparatus
    EP0749770B1|2002-09-04|Device and method for preparing a spray-dried product
    US7128936B1|2006-10-31|Process and apparatus for agglomeration of powders
    US3527647A|1970-09-08|Agglomerating process and apparatus
    US3485637A|1969-12-23|Process for agglomerating coffee
    CN1050485A|1991-04-10|Agglomeration process and device thereof
    US3679416A|1972-07-25|Agglomeration of powdered coffee
    EP0749769B1|2002-01-23|Device for preparing a spray-dried product and method for preparing a product of this kind
    KR970011317B1|1997-07-09|Process and apparatus for treating soluble powdered material
    US2897084A|1959-07-28|Coffee product and method of manufacture
    US4394394A|1983-07-19|Process for producing dry discrete agglomerated garlic and onion and resulting products
    EP0204256B1|1991-12-18|Agglomeration method and apparatus
    US3767419A|1973-10-23|Coffee agglomerates
    US3947166A|1976-03-30|Agglomeration apparatus
    US3804963A|1974-04-16|Process for agglomeration
    US3435106A|1969-03-25|Method for agglomerating powdered material
    US3313629A|1967-04-11|Agglomerating process for powdered food solids or the like
    US3740232A|1973-06-19|Agglomeration of instant coffee
    US3062665A|1962-11-06|Method of producing a preserved egg white product
    SE178819C1|1962-01-01|
    同族专利:
    公开号 | 公开日
    NO862638D0|1986-06-30|
    EP0207384A2|1987-01-07|
    EP0207384B1|1992-05-20|
    CA1252980A|1989-04-25|
    GB2180434A|1987-04-01|
    HU200664B|1990-08-28|
    GB8615147D0|1986-07-23|
    NO166514B|1991-04-29|
    OA08353A|1988-02-29|
    ES8706382A1|1987-07-01|
    NZ216695A|1989-07-27|
    GR861700B|1986-10-31|
    YU43997B|1990-02-28|
    JPS626634A|1987-01-13|
    US4640839A|1987-02-03|
    PH22792A|1988-12-12|
    GB2180434B|1990-03-21|
    DK302386A|1987-01-02|
    DK302386D0|1986-06-26|
    NO862638L|1987-01-02|
    ZA864724B|1987-02-25|
    CN86104893A|1987-05-13|
    PH24468A|1990-07-18|
    IN167178B|1990-09-15|
    PT82872B|1992-10-30|
    KR940008383B1|1994-09-14|
    EP0207384A3|1988-11-23|
    MX164317B|1992-08-03|
    PT82872A|1986-07-01|
    AU585998B2|1989-06-29|
    BR8603042A|1987-02-17|
    CN1005824B|1989-11-22|
    IE861646L|1987-01-01|
    JPH07100020B2|1995-11-01|
    DD247834A5|1987-07-22|
    YU162187A|1988-12-31|
    NO166514C|1991-08-07|
    IE57405B1|1992-08-26|
    DE3685373D1|1992-06-25|
    HUT48441A|1989-06-28|
    ES556319A0|1987-07-01|
    AU5929986A|1987-01-08|
    YU45830B|1992-07-20|
    AT76262T|1992-06-15|
    YU114486A|1988-04-30|
    KR870000869A|1987-03-10|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/750,931|US4640839A|1985-07-01|1985-07-01|Agglomeration process|
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