• 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:
    The invention relates to the food industry and can be used in the continuous thermomechanical processing of liquid masses, mainly cocoa masses. The aim of the invention is to improve the quality of processing liquid masses. The device consists of two identical thin-layer apparatuses of known construction, between which a storage retaining reactor is disposed via pipelines consisting of a cylindrical body 18 in the form of a double casing in which rotor 19 rotates with blades 23 rotating in a gap 22. Sterilization of the liquid masses is carried out in the reactor 5 to 100-150 ° C, preferably 135 ° C, with simultaneous continuous stirring and injection of the mass to a larger volume, and the mass is removed and cooled to 50-100 ° C with the subsequent formation of a thin lo, and before and after removal of part of the mass flow through pump 25 and conduit 27 is returned to the heating step. 2 sec. f-ly, 4 ill.
    公开号:SU1505429A3
    申请号:SU823414908
    申请日:1982-03-19
    公开日:1989-08-30
    发明作者:Шмитт Армин
    申请人:Лува Аг (Фирма)；
    IPC主号:
    专利说明:

    31505
    The invention relates to the technology of food products, namely to the method of continuous thermomechanical processing of liquid masses in a thin layer, mainly mass cocoa, by neutralizing under pressure at temperatures of EO-C, dehydration, degassing, sterilization, aging, final dehydration , degassing and cooling.
    The aim of the invention is to improve the quality of processing liquid masses,
    The method of continuous thermomechanical treatment of liquid masses in a thin layer, mainly mass cocoa, is that the mass is neutralized in a thin layer under pressure at 70-90 ° C, dehydrated, degassing, then sterilization, in which the mass is heated to 100 -150 ° C, preferably 135 ° C with simultaneous continuous displacement and injection of mass to a larger volume, held at these parameters, then finally dehydrated, degassed, removed and cooled to 50-100 ° C (this causes condensation of the vapor phase) after the formation of a thin layer, and before and after removal of the mass of the stream return to the heating stage.
     When the mass is sterilized, the required destruction of the bacteria is provided without adversely affecting it. taste without negative changes in mass (cocoa), while the temperature of the mass is required due to friction or dissipation with a sharp increase in temperature inside the mass
    The average processing time of the mass is determined by the degree of filling; small temperature 1 mass outweighing is compensated by additional heating or cooling of the reactor walls, in which treatment takes place through a double shell.
    Figure 1 shows a schematic diagram of an installation for implementing
    methods; figure 2 - retaining reactor section; Fig. 3 is a radial view of a stapled rotor blade; figure 4 is the same, front view; figure 5 - the blade between the rotor and the inner wall of the retaining reactor, top view; 6 is a diagram (the degree of destruction of microorganisms depending on the temperature of the mass in the supporting reactor).

    0
    50
    five
    0
    five
    The installation (FIG. 1) consists of two identical thin-layer apparatuses 1 and 2. Between these two apparatuses, which are connected by the respective pipelines 3 and A of the product inlet and outlet and the heat transfer fluid, there is a storage retaining reactor 5 (FIG. 2).
    The mass moves from left to right and is carried out with the help of pumps 6-9. From the seed device 10, if necessary, water can be introduced into the mass to be transported via corresponding pipelines 3. At the junction 11
    wires 3 and 4, the so-called static mixers 12 are installed. The heat exchanger 13, by means of which the heat generated in the reactor 5 as a result of friction, is required for sterilization, is maintained in equilibrium, i.e. at the corresponding average level, made in the form of a double casing of the reactor 5, but a separate pass-through heat exchanger 13 can be installed (shown in FIG. 1, dotted line).
    A thermostat 14 (Fig. 2) adjustable inlet and outlet of the coolant is carried out through the respective nozzles 15. The reactor 5 is made up of a cylindrical body provided with inlet and outlet openings 16 and 17 in which the rotor 19 rotates engine work 20.
    The engine 20 and the reactor 5 are mounted on a common support frame 21. The cylindrical rotor 19 limits the annular cylindrical gap 22 from inside, on the surface of the rotor 19 are blades 23, rotating in the gap 22. At the lower end of the rotor 19 are blades, which in combination with the rotor 19 and the bottom 24 of the housing form a pump 25.
    The power of the pumps 6-9 is the same, while the power of the pump 25 is somewhat larger, due to which there is an excess of transported mass. Since this surplus cannot be pumped by pump 8, after which the mass goes to the refrigerator 26, the excess mass through the pipeline 27 returns to the reactor 5, the gap 22 of which is more or less
    filled with mass (theoretically it is possible to fill the entire internal space of the reactor), i.e. the mass is in this reactor not in a thin layer. When the device is put into operation, the installation must be filled to the extent necessary to provide the necessary level of filling of the reactor 5.
    429
    that the range of temperature fluctuations in the mass is minimal, that the average statistical spread of the time for treating particles of a mass relative to a given value is also minimal.
    The amount of mass circulating through conduit 27 was approximately ten times the value
    sa oh
    Measurements have shown that the blades 23 with straight rear edges behind (without protrusions 35) provide
    J5 equal conditions, the conversion of approximately 1/5 of the energy compared to the brackets 28 according to FIG. 3,
    Example 1. A retaining reactor 3 with a height of 2 m and an internal diameter of 0.5 m was used, inside which, with a clearance of 2.5 cm, a rotor 19 with a diameter of 0.45 m rotating at a speed of approximately
    600 min were treated with 1000 kg / h
    25
    Only in this case can pumps | 8 and 9, as well as thin-layer apparatus 2, be able to be run relatively to performance
    The blades 23, which create friction heat in the mass, are made in the form of brackets 28 fixed on the surface of the rotor 19 (Figures 3-5), which are of such dimensions and set so that they touch the cylindrical body 30 with their front edges 9.
    In order to create the strongest possible discontinuity of the flows and thus ensure the formation of vortices, the side posts 31 are installed at a small angle “L to the direction 32 of the flow.
    The vertical flap 33 is set at an angle of | 3 (FIG. 5), its rear edge 34 is provided with a tip 35, which cuts the mass. Due to the fact that the blades 23, together with the rotor 19, rotate in the accumulated mass, an extremely intense turbulence occurs, accompanied by strong heat generation. Heating is perfectly homogeneous, as is the average processing time for particles of the mass. Random, but still possible deviations from this average value are compensated for the temperature with the help of heat exchanger 13, which essentially plays the role of a cooler rather than an additional heater, and in terms of processing time, by returning the mass through the pipeline 27,
    thirty
    cocoa mass.
    The cocoa mass (Bahia) introduced into the first apparatus for thin-layer processing had a water content of 3.5% and an initial acid content with a pH value of 40 mg per 100 g of mass, 0.04%. In line 3, after pump 8, the mass temperature was 60 C. The mass was sent to the thin-layer processing apparatus 1, and also heated to a temperature of 90 C. 5 Here the mass at the indicated temperature was partially dehydrated to 2.4% water content and degassed accordingly. , moreover, the neutralization was carried out by adding an aqueous solution of alkali or water, respectively, by adding 0.6% of water at 80 ° C.
    40
    Then, the mass from apparatus 1 was fed from above using a pump at 90 C to the retaining reactor 5 at a speed of 1 m- / h. The supporting reactor 5 is completely filled, after which, with the rotating rotor 19, the mass temperature is brought to a certain value. Thanks to this, every particle of the mass under pressure in the reactor 5 is subjected to heat for a corresponding duration, which kills the microorganism, i.e. Cumulative reactor 5 allows to achieve optimal results: a high degree of sterilization with minimum processing time and optimum temperature effects on the mass, due to the fact that the reactor provides a sharp increase in mass temperature, i.e. working with high energy density.


    sa oh
    Measurements have shown that the blades 23 with straight rear edges behind (without protrusions 35) provide
    equal conditions, the conversion of approximately 1/5 of the energy compared to the brackets 28 according to FIG. 3,
    Example 1. A retaining reactor 3 with a height of 2 m and an internal diameter of 0.5 m was used, inside which, with a clearance of 2.5 cm, a rotor 19 with a diameter of 0.45 m rotated at a speed of approximately
    regarding the performance of
    600 min were treated with 1000 kg / h
    cocoa mass.
    The cocoa mass (Bahia) introduced into the first apparatus for thin-layer processing had a water content of 3.5% and an initial acid content with a pH value of 40 mg per 100 g of mass, 0.04%. In line 3, after pump 8, the mass temperature was 60 ° C. The mass was sent to the thin-layer processing apparatus 1, and was also heated to a temperature of 90 ° C. Here, the mass at this temperature was partially dehydrated to 2.4% water content and degassed, respectively, moreover, neutralization was carried out by adding an aqueous solution of alkali or water, respectively, by adding 0.6% of water at 80 ° C.
    jg ds to
    Then, the mass from apparatus 1 was fed from above using a pump at 90 C to the retaining reactor 5 at a speed of 1 m- / h. The supporting reactor 5 was completely filled, after which, with the rotating rotor 19, the mass temperature was less than 120 ° C and, moreover, within 1.5 minutes
    jg ds to
    55
    this temperature was maintained at a pressure of 2 bar, and the resulting temperature fluctuations were leveled by means of an external supply and removal of the temperature, for example, through the double wall of the supporting reactor 5. The mass sterilized in this way was continuously supplied using a pump
    At a speed of 1 m / h in a refrigerator 26, cooled therein to 90 ° C, and then sent to a second thin layer processing apparatus 2. The mass had a bactericidal value of g log 1, 8 and an acid content of 0.004%. The resulting cocoa mass was sterilized to a sufficiently high degree and free from the presence of pathogenic microorganisms with an impeccable aroma quality, and it can be directly or after intermediate storage at a certain temperature into a chocolate mass,
    Example 2. The method was carried out in the same device, 950 kg of mass per hour and with the same parameters as in Example 1, however, instead of cocoa mass, a nut mass with 3% water was introduced into the apparatus 1 for thin-layer processing. The temperature in the supporting reactor 5 was raised to 150 ° C at a pressure of 5 bar. The mass was kept and sterilized at the specified temperature for only 1 minute and then cooled in refrigerator 26 to a temperature of 95 C. Even with sufficient aroma quality, which was worse B compared to the weight of example 1, the bactericidal value g was approximately log four.
    Example 3. The method was carried out in the same device, 1000 kg of cocoa mass per hour and with the same parameters as in Example 1, but using a cocoa mass with a water content of 2.45 Z, and after the pump 6, the temperature was maintained. , in the supporting reactor 5, the predetermined sterilization temperature of 110 ° C was maintained at a constant level of 1.7 bar for 1.2 minutes, the mass was sterilized under the specified conditions, and then cooled in a refrigerator 26 to 92 ° C. The treated mass had a bactericidal value log 1.1 (average).
    Fig, 6 shows the preferred range of sterilization according to the experiments, where a is the initial number of microorganisms, b is the number of surviving microorganisms; The optimal sterilization range in the support reactor 5 is cross-hatched. The average residence time is about 1 minute, and the average content at
    about 3%. The initial number of microorganisms is about 1.2-10 microorganisms / g.
    When the temperature of the mass is 120 ° C and the average residence time of the mass in the supporting reactor 5 is approximately 1.5 minutes, a completely cocoa mass with a constant taste and with a final microorganism content of approximately 10,000 is completely free from the presence of pathogenic microorganisms.
    When the temperature of the mass increased by 5-10 ° C in the supporting reactor 5, even the final content of microorganisms of the mass below 50 g was reached, and no significant changes in the taste of the mass occurred.
    The water content of the cocoa mass in the reactor was about 2.5%. Regarding certain parameters, the following should be taken into account. In the proposed method, plant products are processed, which even in one variety, according to their nature, appear to fluctuate in a variety of ways, for example, in oil, water, acid, aroma development, etc. However, such fluctuations can occur not only due to weather conditions, but also the storage conditions and the storage time before processing can affect these parameters.
    five
    0
    five
    0
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    1. A method of continuous thermomechanical treatment of liquid masses in a thin layer, mainly mass cocoa, by neutralizing in a thin layer under pressure with EOR-C, dehydration, degassing, sterilization, aging, final dehydration, degassing and cooling, characterized in that in order to improve the quality of treatment of liquid masses, heating during sterilization is carried out up to 100-150 ° C, preferably 135 ° C, with simultaneous continuous stirring and mass injection to a larger volume, and the mass is removed and cooled to a temperature of 50-100 ° C followed by formation of a thin layer, and before and after removal of part of the mass flow recycled to the heating step,
    2, Device for continuous thermomechanical treatment of liquid masses.
    containing two devices for roHKocj.oft processing of the product, connected with the system for supplying and discharging the product and the coolant in order to improve the quality of processing liquid masses, characterized in that it is equipped with a supporting reactor installed between the devices for thin-layer processing and made a cylindrical housing surrounded by a heat-exchange jacket, inside of which a mixing device in the form of a rotor with blades is located with a gap, and a flow-through refrigerator installed between the supporting reactor and second unit
    28
    X
    /five
    3J 3 / A / g J 4ZV “. four
    five
    0
    for thin-layer processing, with the PCN, the branch pipe of the reactor is equipped with a return pipe, the end of which is connected to the internal cavity of the reactor in its upper part, and the lower part of the reactor at the outlet of the pipe is equipped with a pump, each blade is made in the form of a bracket, the side of which is horizontally and vertically located at an angle to the front rack of the bracket, which is in contact with the inner wall of the cylindrical body, and the rear edge of the bracket is provided with an edge for detachment of the product.
    .S
    ,
    HI
    §
     l and
    §2
    1 t &
    la
    90 WO FIG. 6
    Editor Y. Sereda
    Compiled by N.Miloradova Tehred M.Morgetstal
    Order 5271/58
    Circulation 525
    VNIIPI State Committee for Inventions and Discoveries at the State Committee on Science and Technology of the USSR 113035, Moscow, Zh-35, Raushsk nab., A / 5
    110 120 130
    Tenncpamupa mass - -
    Proofreader V.Kabatsiy
    Subscription
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1505429A3|1989-08-30|Method and apparatus for continuous thermomechanical treatment of fluid masses in thin layer
    GB1347545A|1974-02-27|Distillation apparatus and a method of distillation
    CN207384873U|2018-05-22|A kind of scraper evaporator device with screw conveyor
    US5203970A|1993-04-20|Method for water degasification and distillation
    CN207767453U|2018-08-28|A kind of pasteurize case
    US2536116A|1951-01-02|Method and apparatus for heattreating foodstuffs in containers
    US5215002A|1993-06-01|Single vessel rotary processor
    GB1580742A|1980-12-03|Immersion cooler for cooling milk or other liquids
    US4879132A|1989-11-07|Apparatus for inactivation of enzymes in oil seeds
    US2836589A|1958-05-27|Viscose heating
    KR19980033439A|1998-07-25|Fermentation Dryer and Drying Method
    KR100754978B1|2007-09-04|Rotary type concentrating apparatus with round coil
    JP4849819B2|2012-01-11|Liquid concentrator
    US4279516A|1981-07-21|Container for pasteurizing sludge
    CN215742218U|2022-02-08|Pretreatment equipment for preparing milk powder
    US4406790A|1983-09-27|Method for operating a biological sewage purification plant
    CN214948943U|2021-11-30|Pure steam generator convenient to scale removal
    SU1413126A1|1988-07-30|Apparatus for deodorizing oils and fats
    US1340177A|1920-05-18|Pasteurizer
    US3303870A|1967-02-14|Evaporator apparatus
    CN214388927U|2021-10-15|Steam type rotary drum flaker
    CN212610007U|2021-02-26|Novel circulating water series connection softening equipment
    CN214414020U|2021-10-19|Instant sterilization device applied to tea concentrated solution
    CA1166888A|1984-05-08|Method and plant for the thickening of offal
    JPH10174862A|1998-06-30|Continuous reaction device
    同族专利:
    公开号 | 公开日
    ES8306569A1|1983-06-01|
    PL235560A1|1982-11-22|
    JPH0312859B2|1991-02-21|
    PL131494B1|1984-11-30|
    DD207328A1|1984-02-29|
    GB2095971B|1984-08-30|
    US4446781A|1984-05-08|
    EP0063163B1|1986-01-29|
    HU183860B|1984-06-28|
    GB2095971A|1982-10-13|
    YU212684A|1986-12-31|
    ES510615A0|1983-06-01|
    BR8201531A|1983-02-08|
    DK93882A|1982-09-22|
    CS253568B2|1987-11-12|
    AT17638T|1986-02-15|
    JPS5836342A|1983-03-03|
    US4693904A|1987-09-15|
    EP0063163A1|1982-10-27|
    YU54082A|1985-04-30|
    DE3173596D1|1986-03-13|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2446697C2|2006-12-13|2012-04-10|Аграна Бетайлигунгс- Акциенгезелльшафт|Method for reduction of quantitative content of microorganisms in chocolate mass|US2004009A|1934-06-04|1935-06-04|William A Moir|Method of and apparatus for conditioning chocolate or the like|
    US2589801A|1947-08-28|1952-03-18|Grindrod George|Method for producing cacao-milk beverage material|
    AT245356B|1963-01-11|1966-02-25|Ferdinand Dr Techn Schulz|Process for sterilization bsw. Pasteurization of liquids using cavitation|
    US3384003A|1964-04-20|1968-05-21|Sollich Robert|Apparatus for tempering chocolate and similar fatty masses, particularly for chocolate coating installations|
    DE1977821U|1967-11-29|1968-02-01|Bullmer Bullmerwerk Karl|FABRIC MACHINE.|
    US3638553A|1969-09-04|1972-02-01|Walter Kreuter|Method of treatment of cocoa butter-containing molten chocolate mass|
    US3904777A|1970-07-21|1975-09-09|Nabisco Inc|Process for continuously producing a roasted cocoa mass and for manufacturing a chocolate mass|
    US3885057A|1970-11-27|1975-05-20|Atad|Process for sterilizing a product|
    US3754928A|1972-11-22|1973-08-28|Nestle Sa Soc Ass Tech Prod|Application of compressive and frictional forces in preparing dutchedcocoa|
    DE2313563C3|1973-03-19|1979-04-05|Maschinenfabrik J.S. Petzholdt, 6000 Frankfurt|Process for removing harmful aromas in the continuous treatment of cocoa masses|
    IT1049544B|1974-07-31|1981-02-10|Ducellier & Cie|AUTOMATIC IGNITION ADVANCE DEVICE ACCORDING TO THE SPEED QUOTE OF ROTATION OF AN INTERNAL COMBUSTION ENGINE|
    DE2450515C3|1974-10-24|1981-01-15|Kreucoha Ag, Zug |Method and device for precrystallizing cocoa butter-containing masses|
    FR2452880B1|1979-04-03|1983-07-22|Barry Sa Cacao|
    US4389427A|1980-04-01|1983-06-21|Armin Schmitt|Process for the continuous roasting of cocoa kernel paste|DE3417126C2|1984-05-09|1992-04-30|Werner & Pfleiderer Gmbh, 7000 Stuttgart, De|
    US4667590A|1984-12-10|1987-05-26|Mars, Inc.|Closed food processing system and liquid adjustment apparatus for use therein|
    US5221547A|1989-09-29|1993-06-22|Rossi & Catelli|Heat exchanger method for processing fruits and vegetables|
    IT1260938B|1993-07-21|1996-04-29|Roberto Pellegrin|PROCEDURE AND MACHINE FOR STERILIZING OR DISINFECTING WASTE.|
    DK171666B1|1994-11-18|1997-03-10|Apv Pasilac As|Systems for continuous sterilization of liquids such as milk and cream|
    DE19612957A1|1996-04-01|1997-10-02|Lehmann Maschf F B|Process for the continuous refinement, in particular of cocoa masses|
    US5802965A|1997-02-19|1998-09-08|Lin; Pao-Tseng|Bean sprout processing apparatus|
    DE19721791A1|1997-05-24|1998-11-26|Lipp Mischtechnik Gmbh|Method and device for making chocolate|
    DE19749324A1|1997-11-07|1999-05-12|Hosokawa Kreuter Gmbh|Device for processing cocoa butter-containing or similar fat-containing masses, in particular chocolate mass|
    FR2781647B1|1998-07-31|2000-10-13|Gervais Danone Co|METHOD FOR STERILIZING A FOOD PRODUCT WITH LOW WATER CONTENT, FOOD PRODUCT OBTAINED AND FOOD COMPOSITION CONTAINING THE SAME|
    US6276264B1|1999-10-25|2001-08-21|Dairy Tech Inc|Portable batch pasteurizer|
    US7401546B2|2003-09-09|2008-07-22|Dairy Tech, Inc.|Batch pasteurizer|
    DE102010031047A1|2010-07-07|2012-01-12|Krones Aktiengesellschaft|Device for tempering|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    EP19810102148|EP0063163B1|1981-03-21|1981-03-21|Process and apparatus for sterilisation of ground oil containing fruit seeds such ans cocoa beam, pastes of peanuts, nuts or soja and similar products|
    [返回顶部]