• 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:
    AA finely atomized liquid is projected in a stream and dried by contact with drying gas. The drying gas is projected in turbulent flow from opposite sides of the stream such flow being distributed along the length of the stream. The material may be atomized and projected by a jet of gas issuing from a nozzle, and the drying gas may be projected around the jet so that the drying gas meets the entrainment demand of the jet, thereby preventing recirculation of gases outside the jet.
    公开号:SU1577710A3
    申请号:SU864028157
    申请日:1986-09-02
    公开日:1990-07-07
    发明作者:Туот Джеймс
    申请人:Сосьете Де Продюи Нестле С.А.(Фирма)；
    IPC主号:
    专利说明:

    The invention relates to the field of spray drying, in particular for the processing of food products in the form of a solution, and can be used in the food industry.
    The aim of the invention is to increase the efficiency and speed of drying.
    FIG. 1 shows a schematic of a spray dryer; in fig. 2- - node I in figure 1; on fig.Z - section aa in figure 1 ;. on fig. 4 — device with a working chamber having a straight cross section; in fig. 5 - the same, with several diffuser collector devices and several gas tubes; in fig. 6 - the same, with several sprays of the product.
    The device for spray drying contains a vertical working chamber 1 with an axis 2 and an upper end 3, an atomizer 4 of the product, equipped with an orifice 5 placed in the zone of the upper end 3 of the working chamber 1, a gas tube 6 equipped with a conical transition element 7, a housing
    8 fixed inside the gas tube 6 with the help of centering screws
    9, the supply tube 10, an annular diffuser collector device 11, divided by a transverse partition 7
    mi 12 to conical 13 distributed over height and cylindrical 14 collectors, permeable porous walls 15, container 16 for the foodstuff to be dried, gas source 17 supplied to sprayer 4 of the product, autonomous sources 18 and 19 of drying air, exhaust pipe 20, connected to a cyclone separator 21, a cone-shaped stream of gas 22 with a sprayed product, the mouth of the nozzle 23.
    The spray drying apparatus of FIGS. 1-3) operates as follows.

    five
    0
    5 Q
    five
    The motive gas is supplied from the source 17 to the sprayer 4 of the product and directed by the flow of relatively high flow rates to the nozzle 5. The food intended for drying E is forcibly supplied from the tank 16 through the feeding tube 10. As soon as the solution leaves the lower end of the feeding tube 10, it is immediately caught by the gas passing through the nozzle 5, and sprayed as the gas passes through the neck 23 of the nozzle 5 so that the flow of liquid droplets is removed from the nozzle 5 along with curing movement of gas. The moving gas together with the captured droplets of liquid passes downward from the nozzle 5 in the form of a cone-shaped jet 22, whose axis from the upper to the lower part of the stream coincides with the longitudinal axis 2 of the working chamber 1.
    From the autonomous source 18, the first part of the drying air is supplied to the conical collector 13. Since the collector 13 has very little resistance to flow, the pressure inside the collector 13 will be uniform. Consequently, the porous wall 15 of the collector along its entire circumference will experience a uniform gas pressure. The porous wall 15 has a fairly uniform porosity over its entire circumference; therefore, the drying gas passes through the porous wall 15 mainly at a uniform rate per unit area. Since the pores of the wall 15 are made microscopic and are located close to each other, gas flows from adjacent pores will merge with each other at microscopic distances from the walls of the collector 13 even before
    51
    the stitching gas will meet with the jet. Thus, the upper region of the jet 22 will be surrounded by a continuous stream of drying gas moving radially inward towards the axis of the jet 22 from the outer side of the jet periphery (arrows in FIG. 3). At the bottom of the stream, the drying gas has a low movement speed and moves parallel to axis 2.
    The second part or portion of the drying air is supplied from the source 19, passes through the cylindrical collector 14 and through the wall 15, so that the lower part or the lower region of the jet 22 will be surrounded by an identical continuous flow of drying gas. Adjacent to the junction point of the two collectors 13 and 14 in the zone of the transverse partitions 12, the flow will include drying gas supplied through both collectors 13 and 14.
    The drying gas flows downward along with the propelling gas and the solution droplets. As the liquid droplets pass downstream, the moisture of these droplets evaporates, so that the solution droplets eventually turn into dried particles, and this happens even before they reach the outlet nozzle 20. The particles and gas pass through the outlet nozzle 20 separator 21, where the particles are separated from the gas and removed from the drying system.
    The drying gas supplied through the wall of the shell penetrates the jet and mixes with the movement gas in the jet itself. Moreover, the flow of drying gas in the direction of the jet axis causes the formation of turbulence in the jet itself, and therefore also stimulates the exchange of gases between the central or core region of the jet 22 near this axis and the peripheral region of the jet 22 remote from the axis. This thorough mixing and the continuous introduction of additional quantities of drying gas ensure the presence of gases in all areas of the jet 22 at the desired low humidity, despite the continuous transfer of moisture from the material being dried to the gases.
    The temperature of each part of the drying gas and the temperature ensuring the movement of the gas can be adjusted
    five
    ten
    15
    20
    25
    77
    thirty
    35
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    0
    five
    106
    in an individual way. The first part of the drying gas that is supplied to the conical collector 13 is mixed with the propulsion gas and with the product currently being dried in the upper flow area near the nozzle 5, while the second part of the drying gas supplied to the cylindrical collector 14 is mixed with other gases and product in the lower region of the stream. Thus, it is possible, individually and at the request of the operator, to regulate the input of heat to each region of the jet 22, and consequently, to regulate the temperature regimes of the gas that acts on the product to be dried.
    The positive effects that are achieved through the use of a drying gas with different temperature
    e
    characteristics in different areas of the dryer along the entire length of the stream can be further enhanced by supplying drying air in more than two parts or portions and in more than two areas of chamber 1. For example, three portions of drying air can be supplied to drying chamber 1 at high , medium and low temperatures.
    You can also use different schemes or modes of gas temperature. Thus, if the propelling gas is supplied at a lower temperature than the temperature of the gas that was introduced in the upstream direction, then the temperature of the mixed gases in the immediate vicinity of the nozzle 5 will be low and will gradually increase in the downstream direction within top of the stream. Therefore, during the initial part of the drying process, the temperature of the sprayed product will be very low. This E Zdekt can be enhanced by supplying drying air with a low temperature to the uppermost flow zone and feeding the drying air with a higher temperature to the next flow zone. A low temperature during the initial phases of drying is desirable for those products that are particularly sensitive to heat in the moisture state, but that become less sensitive to heat as they become more and more dried. For example, it is safe to say that coffee and tea extracts become less susceptible to loss of volatile aromatic substances as a result of heating after they acquire a certain degree of dryness.
    In the described embodiments, the flow of drying gas will be symmetrical around the axis of the jet 22. The inward flow of drying air from each part of the annular collector device 11 will be balanced by the same internal flow, but in the opposite direction. These opposite streams of drying air will not deflect the sprayed product from axis 2. Nevertheless (fig. 3), the drying air will always tend to keep the sprayed product at a certain distance from the wall of the shell.
    Stream 22 will tend to capture or entrain the gases surrounding it, and therefore will always strive to form a partial vacuum near the upper end of the jet 22. The partial vacuum, in turn, will always tend to force the surrounding gases to flow upward from the outer side of the jet 22 and recycle. Inward-flowing drying air will prevent the formation of this recirculation.
    Pattern 22 is characterized by a typical or characteristic velocity profile of the gas, with higher velocities occurring in the central region near axis 2, and lower velocities in the (peripheral region far from axis 2).
    In order to minimize the likelihood of wet product sticking to the walls of chamber 1, it is recommended to install the wall of chamber 1 in the upper part of the stream outside the lateral boundary of the jet 22. Any stream does not have discrete or intermittent Physical boundaries, as the jet axis 22 gradually decreases from gas velocity in the downstream direction without any significant gap between the jet and the environment. The lateral boundary of any free jet 22, the integrity of which is not disturbed by the inwardly directed gas flow, is usually determined by the theoretical truncated cone extending along the direction
    0
    five
    0
    five
    0
    five
    0
    five
    the outside of the mouth of the nozzle 5 and having an angle of 23.5 °.
    An important factor is also the pore size of the walls 15. The size and intensity of the vortex motions formed as a result of or as a result of the drying air leaving the pores is directly related to the size of the pores themselves. It can be assumed that the optimal interaction between the vortex motions and the sprayed product occurs when the dimensional characteristic of the vortex movements approaches the diameter of the droplets of the sprayed product themselves. To achieve this dependence, the sizes of individual pores should exceed the average diameter of the droplets in the sprayed state of the product from 0.1 to 10 times, and preferably in the range of approximately 1.0 to 5.0 times. In this case, the pore size means the diameter of the largest rigid spherical particle that will freely pass through the pore. In a spray dryer, the pore size is 30 microns.
    FIG. 4 for now. The scheme of the proposed drying equipment, in which the used nozzle 5 has an elongated rectangular opening, has the same shape and the supply tube 10. The drying chamber 1 also has a rectangular shape (Fig. A).
    The most effective sputtering is achieved when the gas that provides the movement approaches or reaches the sonic velocity in the throat of the nozzle 5.
    As a rule, the motive gas and the drying gas are air, but other gases can be used. Although the drying process usually involves the evaporation of moisture, it is also possible to dry some other products containing other liquids, and not just water. Sugar-based products, such as sugar-water solutions, honey, and molasses, after drying, become sticky, non-crystalline, and remain in this state for a long period of time after the drying process has been completed. To avoid sticking problems during the drying of such products, they can be mixed with other products to form points or centers.
    crystallization and accelerate the crystallization process itself.
    The invention is particularly effective and useful for drying foodstuffs such as milk, water extracts of coffee, chicory and tea, mixtures of these extracts and combinations that include these extracts together with sugar, molasses or honey, using the present invention can be achieved quickly sugaki, the almost complete absence of recirculation inside the drying chamber 1 and controlled product temperatures while maintaining the dried product taste.
    The spray-drying method is carried out under the following temperature conditions. To dry food solutions, the temperature of the gas flowing is maintained at a point above the nozzle 5 downstream of about 500 ° C or less, the temperature of the drying air that is supplied to the upper part of the drying chamber 1 is 120-140 ° C, the temperature of the drying air that is supplied in the lower part of the drying chamber 1, it is equal to 42-103 C. The total mass flow rate of the drying air is maintained 10-20 times higher than the mass flow rate ensuring the movement of the gas.
    Under these conditions, food products can be effectively dried in industrial quantities with a residence time of material in the drying chamber 1 of approximately 50 ms or even less.
    Example. The method was carried out on a device similar to that shown in FIG. 1-3. The neck of the nozzle 5 had a diameter of 18 mm. The collector device 11 had the shape of a truncated cone with a length of 1 m and with an inner diameter of 7 cm at its upper end and with an inner diameter of 33 cm at its lower end. The average pore size of the erases 15 was 30 microns. Aqueous coffee extract with 45% solids was pumped through feed tube 10 at a rate of 70 kg / h. The nozzle 5 was supplied with a flow of air at a temperature of 410 ° C and a feed rate of 267 kg / h. As this air flow passed through nozzle 5, it was cooled by expansion to 310 ° C. In the upper part of the stream filed drying
    with
    x kuya- .s x
    25 20
    and
    a, 577710
    160 air at a temperature of 160 ° C at a rate of 1662 kg / h, and drying air at a temperature of 42 ° C and at a rate of 1948 kg / h was fed to the bottom of the stream. The air and the dried product left the outlet 20 with a temperature of 80 ° C. The coffee extract was dried until particles with a diameter of 20-30 microns and a moisture content of 5% were formed.
    In this case, there was no noticeable deposition and accumulation on the walls 15 of the collector device 11 of the dried product. Experts gave preference to a drink prepared on the basis of this dried product over a drink prepared from a powder obtained from the same extract using the usual method of spray drying. Drink tasting was done anonymously.
    Examples 2-6. The method is carried out on a device which is shown in Figures 1-3. The upper conical collector 13 has an internal diameter of 22 cm at its upper end and 32 cm at its lower end, and the internal diameter of a cylindrical collector 14 is 2 cm. The average pore size in the walls 15 is 30 microns. Before the moment of heating and compression, measure the air flow rate, which is then introduced into the system at room temperature and atmospheric pressure. The pressure and temperature of the gas moving gas are measured directly at the exit of the nozzle 5. The outlet temperature is the temperature of the mixed gases and the dried product in the outlet 20. In each of the examples, 28.300 liters of drying air per minute is passed through the collectors 13 and 14. Other parameters for each example are tabulated.
    Example 7. 44% solid tea extract was dried at a solution feed rate of 115 kg / h, using the apparatus shown in FIG. 1-3. Air was used as propulsion gas and drying gas. The feed rate of the propulsion gas is 317 kg / h, and the total flow rate of drying air is 2860 kg / h, and this flow rate of drying air is equally divided between the collectors 13 and 14. Just above
    thirty
    35
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    45
    50
    55
    I
    the nozzle 5 providing the movement gas had a temperature of 93 ° C, and after its passage through the nozzle 5, the temperature of this gas decreased to 28 ° C. Drying air was supplied to the collector 13 with a temperature of 246 ° C, and to the collector 14 with a temperature of 93 C. Consequently, the sprayed extract was exposed to mixed gases of low, high and medium temperature in the specified sequence. The temperature at the outlet of the working chamber 1 85 ° C. The moisture content in the finished product is 3.5%.
    ExampleB The pre-concentrated milk to a solids content of 48% was dried on the device shown in Figs 1-3. Sco
    the flow rate of the solution is 170 kg / h, and the flow rate of the gas (air) that provides movement is 476 kg / h. The temperature at the outlet of the working chamber is 65 ° С, ° and the moisture content in the final product is 5%.
    To implement the method of spray drying, you can also use the device shown in figure 4-6.
    FIG. Figure 4 shows a device whose working chamber 1 is rectangular in cross section, the nozzle 5 has an elongated rectangular opening-i, and the supply tube 10 having a rectangular outlet opening is installed directly inside the nozzle 5. The nozzle 5 is placed between the porous walls 15, expanding by157
    The design of the drying equipment (FIG. 5) includes the pain number of annular diffuser collector devices 11 in the shape of a truncated cone and gas pipes. Each gas tube 6 is positioned in such a way that precisely fills the movement of gas in the associated collector gas. The device 11 is through a nozzle, and the liquid material intended for drying is supplied through a supply pipe (not shown) directly to the gas pipe. The drying gas supplied through the working chambers (shown), which surround the collecting devices 11, is introduced through the latter. Therefore, each
    from the outside towards the lower end of the working chamber 1. The gas that provides movement, which is supplied to the nozzle 5 from these collector devices 11, picks up and sprays vegetation in exactly the same way,
    ,,
    ten
    20
    25
    771012
    Py I is applicable to the embodiment (Fig. 4), in which a nozzle 5 of a non-circular cross section is used. In the case of using a rectangular nozzle 5 (Fig. 4), its diameter is used as its dimensional characteristic. The jet coming out of the rectangular nozzle 5 expands outwardly in the same way as the jet coming out of the circular nozzle 5 (Figures 1-3). The theoretical lateral boundary of the free jet leaving the rectangular nozzle and which is not influenced in any way by the inward flow of gas has an obelisk shape, the lateral sides of which extend from the edges of the nozzle 5, and the opposite sides of the same obelisk are angles 23.5.
    The design of the drying equipment (Fig. 5) includes a large number of truncated cone-shaped annular collector devices 11 and gas tubes 6. Each gas tube 6 is positioned in such a way that it directly guides the movement gas to the associated collector device 11 through a nozzle, and the liquid material to be dried is fed through a feed tube (not shown) directly into each gas tube. Drying gas supplied through working chambers (not shown) that surround the collector devices 11 is introduced through the latter. Therefore each
    thirty
    35
    until of these collector devices 11 acts exactly the same way
    a thief that is supplied to the feed tube 10. The gas leaves the nozzle 5 in the form of a jet of rectangular cross section; This gas carries a stream of particles or droplets of the sprayed product. Drying air is supplied by narrow and wide porous walls 15. As in the case shown in FIG. 1-3, in this case, the jet is completely and completely surrounded by drying air introduced inwards through the porous walls 15 and the sprayed product passes between oppositely directed inward streams of drying air.
    The mentioned dependencies between the requirement of capturing or increasing the jet and the flow rate of the drying gauch through the working chamber
    as well as the upper part of the working chamber 1. The jet coming out of each nozzle is completely surrounded by 5 (throughout the upper part of its length) an inward-directed drying gas. The lower ends of the collector devices 11 are located between a pair of oppositely installed porous walls 15, an additional amount of drying gas is supplied through the collector 13 through these porous walls 15.
    Gases and sprayed material leaving the collector device 11, pass between the oppositely directed inward flows of the drying gas supplied from the porous walls 15 (arrows in Fig. 5), the drying gas,
    five
    Produced from these walls 15, under turbulence conditions, are mixed with the sprayed material and with the gases that are released from the collector devices I1. The gas and sprayed streams leaving the collector devices 11 will not be completely surrounded by inward drying gas as they pass between the porous walls 15. To minimize the likelihood of recirculation in areas between adjacent streams, it is recommended to use such the configuration of the collector device 11 and the flow of drying gas through these porous walls 15, which ensures almost complete dispersion of the jet exiting each nozzle within its associated (jet d) collector device P. Therefore, it is preferred that each collector device 11 extends downward from a corresponding (associated with it) nozzle for a distance that is at least 10 times larger than the diameter of the nozzle, and the drying gas is best flow through each collector device of 1 G at a speed which will be at least equal to the theoretical requirement for capturing or dragging a jet.
    In the described embodiments of the invention, the material is introduced into the jet providing the movement of the gas. However, the same material can be sprayed and injected without the use of propulsion gas. The equipment (Fig. 6) includes a working chamber 1, which is closed at its upper end and on its sides. The contours of these two sides of the working chamber 1 are determined by the configuration of the diffuser collector device 11. Each porous wall 15 communicates with collectors 13 and 14, which are connected to gas sources (not shown). Sprays 4 are installed in the upper wall of the working chamber 1. Each sprayer 4 has a large number of small holes opening towards the inside of the working chamber 1. These nozzles 4 are connected to a gas source 17 made, for example, in the form of a high-pressure pump.
    Designed for drying the liquid using a source of 17 pro
    ten
    15
    20
    25
    five ,,.
    35
    40
    five
    0
    chases through the nozzles 4, with the result that a stream of fine particles or droplets of this liquid flows down from each nozzle 17. The drying gas supplied through the collectors 13 and 14 is introduced through the porous walls 15 and directed to the flows of the liquid droplets. These streams of liquid droplets flow between opposing inward streams of drying gas dispersed along the entire length of the streams, due to which, under the conditions of turbulence, the sprayed liquid is subjected to an effective effect of the drying gas. It is recommended that the porous walls 15 and, therefore, oppositely directed inward flows of drying gas extend downwards beyond the point where the material will be essentially already dry.
    Since the upper end of the working chamber 1 is closed, the continuous flow of drying gas in the working chamber 1 causes the material to be dried to be lowered. The dried material is collected in a separator (not shown), which is connected to the lower end of the working chamber 1.
    Since in this case there are no jets that allow the movement of gas, there is no need to arrange the flow of drying gas so that it eliminates the likelihood of recirculation, which is usually caused by the jets mentioned. Consequently, the streams of droplets or particles of the material will not be completely and completely surrounded by the inward drying gas. In addition, the heat required to ensure the drying is provided entirely and completely by the drying gas. In this case, you can use any spray liquid nozzle capable of providing the required degree of spraying. In all other aspects, the drying operation will be identical to that described.
    权利要求:
    Claims (3)
    [1]
    1. Method of spray drying a food product in the form of a solution containing at least 40 wt.% Solid particles selected from the group of components, including milk, coffee extract, chicory extract, tea extract, mixtures thereof, or mixtures of several of the above components with sugar,
    molassa or honey, which consists in mixing the drying air with a turbulent flow of the sprayed product by distributing drying air into the flow from opposite sides along the last transverse introduction of the sprayed air to the inside, with full coverage of the initial portion of the flow, and In order to increase the efficiency and speed of drying, the drying air is supplied to the upper part of the stream with a temperature of 120-246 ° C, mostly 120 ° C, and to the lower part - from 42 to 103 ° C, continuously 80 ° C ,.
    [2]
    2. Method according to claim 2, characterized in that the product is sprayed with gas to form droplets with an average diameter of 16-63 microns.
    [3]
    3. Device. For spray drying a food product, containing a vertical working chamber with coaxially mounted in its upper end
    312 (103) 6800 170
    153 (98) 6800 170
    316 (104) 3680 139
    324 (103) 3680 120
    248 (108) 3680 144
    a product spray in the downward direction, equipped with a turbuliator, an annular diffuser collector swept in height, connected to at least one source of drying air through a supercharger and made with opposing output permeable porous walls framing the chamber, extending in the direction of flow of the sprayed product , with the pores of the walls directed transversely relative to the axis of the chamber, and the walls in the upper part cover the chamber along the entire perimeter, o In order to increase the efficiency and speed of drying, the annular collector device is additionally divided by transverse partitions into collectors distributed in height, each of which is connected to its own independent source of drying air, and the permeable porous walls are made with a pore size of 30 microns .
    103 92 3.66 (50) 67
    91 85 No data (63) 34
    86 95 2.6 (29) 33
    85 84 2.6 (16) 19
    62 77 4.27 (27)
    No data
    №F
    at
    I I
    s si
    tlr
    901Ш51
    1577710
    eleven
    Compiled by N. Isachenko Editor L. Gratilo Tehred M. Hodannch Corrector M. M Aksimishinets
    Order 1857
    Circulation 594
    VNIIPI State Committee for Inventions and Discoveries at the State Committee on Science and Technology CC / CP 113035, Moscow, Zh-35, 4/5 Raushsk Nab.
    Production and Publishing Combine Patent, Uzhgorod, st. Gagarin, 101
    FIG. 6
    Subscription
    类似技术:
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    同族专利:
    公开号 | 公开日
    PT83291A|1986-10-01|
    IE862091L|1987-03-03|
    EP0214441B1|1991-08-07|
    GB2179562A|1987-03-11|
    HU199662B|1990-03-28|
    DK165278C|1993-03-22|
    JPH07112521B2|1995-12-06|
    DD249412A5|1987-09-09|
    GR862243B|1987-01-02|
    CA1271123A|1990-07-03|
    EP0214441A3|1988-03-30|
    IL79671D0|1986-11-30|
    YU44090B|1990-02-28|
    AR240986A2|1991-04-30|
    EP0214441A2|1987-03-18|
    DK334386A|1987-03-04|
    MX165393B|1992-11-10|
    IE59586B1|1994-03-09|
    DE3680731D1|1991-09-12|
    PH24487A|1990-07-18|
    AU6012286A|1987-03-05|
    US4702799A|1987-10-27|
    IN167637B|1990-11-24|
    PT83291B|1993-03-31|
    YU130387A|1988-12-31|
    JPS6257601A|1987-03-13|
    ES2002732A6|1988-10-01|
    CN86106073A|1987-03-04|
    BR8604204A|1987-04-28|
    YU152686A|1988-04-30|
    HUT45876A|1988-09-28|
    GB2179562B|1989-08-31|
    AT65929T|1991-08-15|
    NZ216849A|1989-05-29|
    AR240986A1|1991-04-30|
    KR870003365A|1987-04-16|
    AU577021B2|1988-09-08|
    ZW15986A1|1986-10-29|
    YU44592B|1990-10-31|
    DK334386D0|1986-07-14|
    DK165278B|1992-11-02|
    GB8618992D0|1986-09-17|
    ZA865920B|1987-03-25|
    CN1005212B|1989-09-20|
    KR940008435B1|1994-09-14|
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