WO2015065228A1 - Procédé d'évaporation de produits en écoulement et dispositif d'évaporation pour sa mise en œuvre - Google Patents

Procédé d'évaporation de produits en écoulement et dispositif d'évaporation pour sa mise en œuvre Download PDF

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Publication number
WO2015065228A1
WO2015065228A1 PCT/RU2013/000969 RU2013000969W WO2015065228A1 WO 2015065228 A1 WO2015065228 A1 WO 2015065228A1 RU 2013000969 W RU2013000969 W RU 2013000969W WO 2015065228 A1 WO2015065228 A1 WO 2015065228A1
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Prior art keywords
product
tank
circuit
evaporation
pump
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PCT/RU2013/000969
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English (en)
Russian (ru)
Inventor
Владимир Григорьевич МАКАРЕНКО
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Владимир Григорьевич МАКАРЕНКО
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Priority to PCT/RU2013/000969 priority Critical patent/WO2015065228A1/fr
Publication of WO2015065228A1 publication Critical patent/WO2015065228A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying

Definitions

  • the invention relates to methods for heat treatment (evaporation) and concentration of fluid products using various equipment.
  • any flowing products and mixtures can be subjected to heat treatment with evaporation.
  • Evaporation is the removal of an excess amount of the most volatile components, in particular water or other solvents, from a complex product, and is used to give the product the required composition and the desired physicochemical properties, including those necessary rheological properties. As a rule, evaporation is accompanied by heating of the concentrated product.
  • the heat exchange surface can be the wall of the container with the product or the surface of a heating element of an arbitrary design immersed inside the tank.
  • a technically more advanced flash cooking is boiling under reduced pressure.
  • There is a known method of filling (Patent RU 2432537, IPC F26B9 / 06, F26B5 / 04, publ. 10/27/2011), which can significantly remove the problem of soot and overheating of the product, but requires much more complex and expensive equipment. Evaporation of foaming products in this way also causes additional technical difficulties.
  • a significant decrease in the boiling point requires a significant vacuum and the use of a coolant for condensation of vapors, and this, in turn, affects the increase in the cost of the finished product.
  • a number of methods are known in which the evaporation of a volatile component is carried out without boiling due to the contact of the product with a “dry” gas medium.
  • the effective operation of these methods requires a significant free surface of the product and a low relative vapor pressure of the removed component (for water vapor, relative humidity) above it.
  • the product is usually heated either by an arbitrary solid-state heater, or by contacting the product with a heated gas medium.
  • it is required to be carried out in special evaporation devices, which necessarily create a significant contact area of the product with the gaseous medium.
  • evaporation devices can be divided into the following classes:
  • the film apparatus according to the patent RU 2223130 allows for the implementation of boiling without a boiling process, which means at a lower temperature. At the same time, to lower the evaporation temperature, it is necessary to forcefully remove the vapors, ensuring the circulation of the gaseous medium above the surface of the product.
  • the treatment is carried out using heat generated by liquid friction, which is created by mechanical the proper circulation of the product in a heat treatment device with at least one mechanical heater.
  • the device includes a bearing assembly with a vertical drive shaft, a drive and a heater.
  • This device describes a submersible type mechanical heater according to patent j ⁇ s2267350, with an additional function of dispersing and homogenizing the product.
  • the disadvantage of this device is its low efficiency at a product temperature close to the boiling point, and, as a result, the inability to use the product to be concentrated for concentration in cases where it is necessary. It also makes it difficult to process products prone to foam formation.
  • the problem solved by the present invention is the development of a heat treatment method with evaporation of highly viscous and foaming products, which allows to obtain an extensive range of high quality products, and the development of compact and high-performance devices for implementing this method.
  • the problem is solved using the method of boiling fluid products, including the circulation of the product in the tank, and its heating.
  • the product is circulated through the evaporator circuit 2, which includes at least one pump 3 for collecting the product from the tank 1 and to ensure its circulation in the evaporator circuit 2, at least one heating a body 5 for ensuring the heating of the product in the complete circuit 2 and at least one injection device 4 for the reverse injection of the product into the tank and connected in series by pipelines, part of the product is forcibly taken from the tank 1 to the evaporation circuit 2, it is heated in the heater 5 paired circuit 2, and the heated product is injected back into the upper part of the container 1 above the surface of the product.
  • the total power released by the heaters 5 in the evaporation circuit at the stage of evaporation of the product satisfies the condition:
  • W is the total power (W) emitted by the heaters
  • W * is the total heat loss power (W)
  • ⁇ is the product heating rate (° C / s)
  • C is the product heat capacity (J / (kg- ° C))
  • m is the mass of the product subjected to heat treatment (kg)
  • the evaporated components of the product are indexed i
  • q is the specific heat of evaporation of the / -th component (J / kg)
  • Mi is the required rate of evaporation at the temperature of the process (kg / s) .
  • T depends on the course of the evaporation process, that is, on the last component of the inequality.
  • the heater 5 meets the requirement:
  • the heater 5 satisfies the requirement:
  • a vacuum is maintained in vessel 1 during evaporation of the product.
  • the container 1 is vented with dry gas or air when evaporating the product.
  • an evaporation device for evaporation of current products including a tank 1 with inlet and outlet openings, a heater 5.
  • the device includes at least one evaporator circuit 2, which includes at least one pump 3 for collecting the product from the tank 1 and ensuring its circulation in the circuit 2, at least one heater 5 to ensure heating of the product in the evaporative circuit 2 and at least one injector device 4 for reverse injection of the product into the tank 1 and connected in series by pipelines, the injector device 4 is installed in the upper part of the tank 1 above the level of filling with its product.
  • the total power released by the heaters 5 in the evaporation circuit 2 at the stage of product evaporation satisfies the condition: where Wi is the total power (W) emitted by the heaters 5, W * is the total heat loss power (W), T is the product heating rate (° C / s), C is the product heat capacity (J / (kg- ° C) ), m is the mass of the product subjected to heat treatment (kg), the evaporated components of the product are indexed /, the specific heat of evaporation of the / component (J / kg), and the required rate of evaporation at the process temperature (kg / s).
  • the heater 5 meets the requirement:
  • the heater 5 satisfies the requirement:
  • a sprinkler device or a valve with or without a sprinkler nozzle an adjustable flow nozzle or an adjustable valve or throttle mounted on the upper wall of the tank 1 are used to form a gap between the injection device 4 and the product surface in the process capacity 1.
  • the pump 3 and the heater 5 in the upper circuit 2 are made as a single device.
  • the injector device 4 is at the same time a hydraulic throttle to create overpressure in the evaporator circuit 2 and to prevent boiling of the product therein.
  • the injector device 4 is provided with a valve for regulating the pressure in the upper circuit 2 and increasing the temperature of the product therein.
  • a filter separator 6 of lump inclusions in the evaporated product is installed at the inlet to the evaporator circuit.
  • a breather is installed in the lid of the process vessel 1
  • the process vessel 1 is provided with a stirrer.
  • the process vessel 1 in its upper part is connected to a vacuum line 8 for removing steam.
  • the vacuum line includes a steam condenser 10.
  • the upper part of the container 1 above the product is connected to a closed or open ventilation circuit.
  • the ventilation circuit 11 includes a fan 12 and at least one gas or air conditioning device 13.
  • the conditioning device 13 includes a purification filter 14 and / or a desiccant 15.
  • the problem is solved using a device for heat treatment and embedding of fluid products, including a bearing assembly 16 with a vertical drive shaft 17 and a drive.
  • the device comprises a complete contour, which includes a pump 21, at least one injector device 26, which closes a complete contour, connected by a pipeline line, for mounting the evaporative circuit elements in the lower part of the bearing assembly 16 together with it or separately, the supporting flange 19, under the bearing node 16 is a console 20 of an arbitrary design, on which the pump housing 21 is mounted coaxially with the drive shaft 17, the pump 21 consists of a fixed detachable housing 23, mounted on the console 20 and the rotor 24, installed on the drive shaft 17, the pump 21 has a Central inlet 22 for intake of the product and at least one outlet from the pump 21 for supplying the product through a pipe line to the injection device 26 for the reverse injection of the product into the container.
  • the inlet of the pump 21 is located below the level of the product in the tank, and the outlet of the injection device 26 is located above the level of the product in the tank.
  • the overall circuit is provided with diverting valves 28 for forcibly unloading the product and / or feeding it back into the container through the jet mixing device.
  • the device is equipped with a sensor 30 for detecting the temperature inside the vessel and a sensor 31 for detecting the temperature inside the vapor circuit.
  • the senor 31 is installed in the closing part of the evaporator circuit, upstream of the injection devices 26.
  • the injector device 26 is a hydrodynamic throttle.
  • the injector device 26 is provided with a control valve 32 for controlling the instantaneous flow rate of the product through the evaporator circuit.
  • the injector device 26 is in the form of a rain device, a nozzle or a control valve 32 fixed to the support flange 19.
  • a stabilizer 33 is mounted on the bottom of the pump housing 21, which comprises fixed radial vanes 34 and a non-metallic plain bearing 35 to support the end of the shaft 17.
  • a strainer 36 is installed at the pump inlet.
  • a chopper knife 37 is mounted on the pump shaft in front of the inlet.
  • centrifugal pump 21 a rotary disperser having pump functions is used as the centrifugal pump 21.
  • variable speed drive is used as the drive.
  • the evaporator circuit is provided with two injection devices 26.
  • the piping line consists of at least one outlet pipe 25 from the pump 21, which is connected to a pipe 27 for collecting products from the outlet pipes 25 to the injection device 26 closing the evaporator circuit.
  • the evaporator loop pipelines 27 are located above the support flange 19. Preferably, the evaporator loop pipelines 27 are located below the support flange 19.
  • the device is provided with two outlet pipes 25 for discharging the product from the pump 21 through the outlet openings of the pump 21 located symmetrically with respect to the axis of rotation of the drive shaft 17.
  • a filter separator for piecewise inclusions can also be installed at the inlet to the evaporator circuit.
  • the evaporator injector device is installed in the upper part of the tank above the level of filling with its product.
  • the type of injection device is selected depending on the properties of the product. It can be a dozhdevalny device, a nozzle, or simply an adjustable valve fixed on the upper wall of the tank.
  • the minimum required clearance between the injector device and the surface of the product must ensure the normal course of the cooking process. For each specific product, it is determined empirically.
  • Evaporative circuit elements including pipelines, can be located both outside and inside the product container.
  • the choice of the location of the evaporation circuit is carried out in the design of a particular evaporation plant.
  • the container can be equipped with a mixing device of any suitable type.
  • a single evaporative circuit here means a simultaneously controlled and coordinated functioning set of the necessary equipment listed above, regardless of the number of devices of each type installed in it.
  • the evaporation process takes place directly in containers from the surface or above the surface of the product. Due to the need to remove vapors, the volume above the surface of the product communicates with the atmosphere, preferably through a valve or breather, or is evacuated, or ventilated with dried gas or air.
  • the first two of these options involve boiling the product, and in the scheme with tank ventilation, the boiling process may not be used.
  • Evaporation is carried out using the heat generated by the heater in the evaporation circuit.
  • the heater satisfies the requirement:
  • W Z W * + T - C - m + T q r Mi. (2)
  • Wz is the total power released by the heaters (W)
  • W * is the total heat loss power (W)
  • T is the heating rate of the product (° C / s)
  • C is the heat capacity of the product (J / (kg- ° C))
  • m is the mass of the product subjected to heat treatment (kg)
  • the evaporated components of the product are indexed / numbered, is the specific heat of vaporization of the ⁇ ' - ⁇ component (J / kg), is the required rate of evaporation at the process temperature (kg / s )
  • the task of preparing products of this variety with consistently high quality is solved in the most technically simple implementation the proposed method.
  • the product is evaporated by boiling and spontaneously displacing the vapor into the atmosphere.
  • the product is forcibly taken from the tank, heated in the outlet circuit and injected back into the tank through the injection device. Due to heating in the circuit, the product injected from above has a higher temperature than the one in the tank.
  • the injector device is designed in such a way as to serve as a hydraulic throttle, for example, it is equipped with a control valve that allows creating an excess pressure in the circuit that is sufficient to prevent boiling of the product.
  • the residual slow boiling in the surface layer of the thick product can lead to its microporous structure and to undesirable deviations in its rheological and organoleptic properties. So, hot caramel acquires visco-elastic properties, which is undesirable in technology, and lollipop caramel loses its transparency, acquires a milky color and becomes rough when resorbed, i.e. losing its consumer qualities.
  • the operation mode of the evaporator circuit is selected so that it satisfies the condition:
  • the process is carried out with boiling of the product, and evacuation only lowers the boiling point. All the conditions and patterns of operation of the outlet circuit disclosed in the previous example remain valid, but the design of the entire integrated device is complicated.
  • the container for the product is sealed, and in the upper part, a vacuum steam line is connected to it, in which a suitable vacuum pump and, if necessary, a steam condenser are installed. With sufficient performance of the vacuum pump (usually at low vacuum), a steam condenser may not be installed in front of it.
  • the vapor pressure of the component removed from the product always remains below the pressure in the product and boiling does not occur.
  • the evaporation device When evaporating according to this variant of the method, the evaporation device is equipped with a tank ventilation circuit, which can be open to the atmosphere or closed. When using an open ventilation circuit, the air entering it must be cleaned to avoid product contamination. When using a closed loop, it is possible to ventilate the tank with any gas inert to the product, and the gas must be drained, i.e. remove from it a pair of volatile product component. In both cases, a rather complicated additional equipment is required.
  • evaporation with tank ventilation allows the process to be carried out at a lower temperature, which for some products may simply be a necessary condition for their preparation. This already justifies a significant complication of the evaporation plant, and makes such an embodiment of the evaporation method industrially applicable.
  • any evaporation device according to the proposed method contains an obligatory element - an evaporation circuit, the best implementation of which, according to the author, can be indicated.
  • FIG. 1,2,3, in FIG. 4 shows a device for heat treatment and boiling up of fluid products, including the necessary components of the evaporation circuit, and suitable for use as part of the evaporation device according to any of the schematic diagrams shown in FIG. 1,2,3.
  • Figure 1 shows a diagram of an evaporation device in the simplest embodiment of the invention.
  • Evaporation (concentration) of the liquid product in tank 1 is carried out with the product circulating through the evaporation circuit 2, which, in addition to the necessary pipelines, includes:
  • injection device 4 for reverse injection of the product into the container
  • heater 5 to provide additional heating of the product in the loop and intensification of the evaporation process.
  • a mechanical heater is used, combined with the pump in one device.
  • the heater satisfies the requirement:
  • the operating mode of the outlet circuit is selected so that it also satisfies the condition:
  • the injector device 4 of the complete circuit is installed in the upper part of the tank 1 above the level of filling with its product.
  • the type of injection device is selected depending on the rheological properties of the product and can be any. But in order to exclude boiling inside the overall circuit, as well as to be able to regulate the instant consumption of the product in it in order to ensure conditions (1) and (3), the injection device is endowed with the function of an adjustable hydraulic throttle.
  • the injection device is a variable flow nozzle, or simply an adjustable throttle or valve with or without a sprinkler nozzle.
  • the minimum required clearance between the injector device and the product surface should ensure the normal course of the evaporation process. For each specific product, it is determined empirically.
  • W is the total power released by the heaters (W)
  • W * is the total heat loss power (W)
  • G is the heating rate of the product (deg / s)
  • C is the heat product capacity (J / (kg-deg))
  • index i numbers the evaporated components of the product, is the specific heat of evaporation of the ⁇ ' component (J / kg)
  • / is the required rate of evaporation at the temperature of the process (kg / s).
  • the concentration of fluid products with lump inclusions at the entrance to the evaporator circuit is installed filter separator lump inclusions 6.
  • the container is closed, and in its upper part, if necessary, a breather 7 is installed.
  • the tank is equipped with a mixing device of the appropriate type.
  • the mixing device can be any, both mechanical and inkjet.
  • Figure 2 shows a diagram of an evaporation device using evacuation.
  • the boiling point at atmospheric pressure is too high and fatal for the product, it can be lowered by lowering the total hydraulic pressure, i.e. using evacuation. For this, the evaporation device shown in FIG. 2.
  • a container 1 with the product is sealed and a vacuum line 8 is removed to its upper part, containing at least one vacuum - pump 9 of the required capacity.
  • a steam condenser 10 is also installed in front of it in the steam exhaust line. In this case, the parameters of the vacuum pump and condenser are selected in concert to ensure the required steam productivity.
  • Fig. 3 shows a diagram of an evaporation device using tank ventilation.
  • the product needs to be concentrated at a very low temperature. Boiling with boiling at this temperature may require a too significant reduction in hydraulic pressure, up to the technical impracticability of the boiling process due to the impossibility of normal operation of the hydraulic devices of the evaporator circuit (pump, mechanical heater) and unreasonably high performance requirements for vacuum equipment. Nevertheless, filling at such a low temperature is still possible by the proposed method, but without boiling the product, using forced ventilation of the container with the product.
  • Air conditioning includes, at a minimum, gas purification if the ventilation circuit is not open, and gas drainage (condensation of the vapor of the removed component) if the ventilation circuit is closed.
  • a schematic diagram of the evaporator is shown in FIG. 3.
  • a ventilation circuit 11 containing a fan 12 and at least one conditioning device 13 is connected to the upper part of the tank 1.
  • the conditioning device may include a cleaning filter 14, or a dehumidifier (condenser) 15, or both of these devices.
  • FIG. 4 shows a front view of a device for heat treatment and evaporation containing the necessary elements of the evaporation circuit, with a section of the immersion part.
  • the shown device variant contains: - Bearing assembly 16 with a vertical drive shaft 17, as well as a pulley or coupling half 18 mating with the drive in the upper part;
  • An arbitrary design console 20 located under the bearing assembly for mounting the pump housing 21 on it coaxially to the drive shaft 17.
  • a centrifugal pump 21 with a central inlet 22 for withdrawing product from the tank and at least one pump outlet opening connected to the evaporator outlet pipe 25 contour.
  • 21 includes a fixed detachable housing 23 mounted on the console 20, and a rotor 24 mounted on the drive shaft 17;
  • At least one outlet pipe 25 for draining the product from the pump 21 through the outlet of the pump and supplying the product further along the evaporation circuit.
  • the device has two outlet openings and two outlet pipes arranged symmetrically with respect to the axis of rotation of the drive shaft. The symmetrical arrangement of the pump outlets associated with the outlet pipes 25 significantly reduces the bending load on the cantilever drive shaft and its runout during operation;
  • At least one injector device 26 for reverse injection of the product into the container
  • - Injector device 26 is located in the upper part of the tank, above the level of filling with its product.
  • the technological capacity is closely mated with the flange 19, which closes the technological capacity.
  • the length of the immersion part of the device in the tank and the height of the tank are selected so so that the inlet 22 of the pump 21 is preferably near the bottom of the tank, and the product level is lower than the outlet openings of the injection devices 26.
  • the rotor 24 of the pump 21 is driven into rotation by the drive shaft 17 through a pulley or coupling half 18 from an electric drive mounted on a bearing assembly 16 or on a frame external to it.
  • the pump 21 circulates the product through the evaporator circuit, the injector device 26 (or devices) located above the free surface of the product allows it to be evaporated. If the drive coupled to pump 21 provides a rotational speed and power transmitted to the product that fully or substantially satisfies relation (2), pump 21 also heats the product, i.e. serves as a mechanical heater.
  • the evaporator circuit of the device contains taps 28, equipped with shut-off valves for forcibly unloading the product from the tank or feeding it back into the tank through the jet mixing device (not shown in FIG. 4).
  • the evaporator circuit has detachable couplings 29 for incorporating an external heat exchanger, flow heater, or other special-purpose device into it.
  • the device is equipped with a product temperature sensor 30 inside the tank and a temperature sensor 31 inside the evaporator circuit, and the temperature sensor 31 is preferably installed at the end of the evaporator circuit upstream of the injection devices 26.
  • the injection device 26 is a hydrodynamic throttle, and to control the heating and evaporation conditions, the injection device is additionally equipped with a control valve 32, which allows controlling the instantaneous flow rate of the product through the vapor circuit and its temperature increment relative to the temperature in the tank.
  • the type of injection device is selected depending on the properties of the product. This can be a sprinkler device, a nozzle, or simply an adjustable valve mounted on the support flange of the device.
  • the device is equipped with a stabilizer 33, which is mounted on the lower part of the pump housing 21 having an inlet 22 and contains fixed radial vanes 34 and preferably non-metallic plain bearing 35 to support the end of the shaft 17.
  • a mesh filter 36 made of sheet metal is installed in front of the inlet 22 to the pump 21, preventing large piecewise inclusions from entering the pump.
  • the optimum filter cell size depends on the requirements for the product and the technical capabilities of the pump and the evaporation circuit devices.
  • the mesh filter is preferably removable with the possibility of replacement in order to be able to change the cell size when processing various products on one device.
  • a chopper knife 37 can also be mounted on the shaft 17 of the pump 21 in front of the strainer and inlet 22 for preliminary crushing of large lumps in the product.
  • the chopper knife 37 is preferably made of sheet metal and has a shape similar to that shown in FIG. 5.
  • FIG. 5 shows a chopper knife 37 for the device of FIG. four.
  • the chopper-knife 37 On the shaft 17, the chopper-knife 37 is installed so that when the shaft rotates, the elongated knife body located in the plane of rotation clears large inclusions that have not passed into the filter from the screen and thereby prevent clogging of the filter and the occurrence of a hydraulic jam that interferes with the normal operation of the device .
  • crushing of lump inclusions is provided by the bent ends of the chopper-knife 37 moving at a high speed.
  • the product rotation created by the chopper-knife 37 is damped by the closely located stationary blades of the stabilizer 33.
  • a rotary dispersant having pumping properties can be used as a centrifugal pump 21, for example, the rotary dispersant according to patent No. 2156648.
  • the disperser rotor is installed on the pump shaft, and its stator is installed in the pump casing.
  • the proposed device for heat treatment and evaporation is driven by a common industrial electric motor of a fixed frequency.
  • this drive option is quite acceptable. Otherwise, it is much more convenient to feed the electric motor with an alternating current of variable frequency using the corresponding frequency converter. This makes it possible to change the rotation frequency of the pump shaft, and therefore the active power transferred to the product.
  • the speed of the motor and pump shaft it is always possible to ensure the optimal heat treatment mode for a particular product, even if its properties change greatly during such processing.
  • the device in the best embodiment is equipped with a stabilizer 33 and two outlet pipes 25. This allows to reduce vibration and permanent deformation of the drive shaft 17 of the pump 21, to reduce noise and the nose of the rubbing parts of the device.
  • the injection circuit injection device 26 is a hydrodynamic choke, which prevents the product from boiling inside the circuit.
  • the device is equipped with means for monitoring and controlling the operating mode, which include at least two temperature sensors 30, 31 (in the tank - sensor 30 and in front of the injection device - sensor 31), allowing measure the temperature increment of the product in the evaporator circuit, and a control valve 32 in the injector device 26, which allows changing the magnitude of this increment due to a change in the instantaneous product flow in the circuit.
  • the device is used for the preparation of a wide range of products, or the product significantly changes its properties during processing, in addition to the above mentioned means of monitoring and control, the device is equipped with an appropriate electric variable speed drive. This allows you to adjust the power of mechanical heating by changing the frequency of rotation of the pump shaft and to process the product always with optimal power and maximum possible productivity.
  • the evaporator circuit is equipped with at least two injection devices 26 (Fig. 4) and a shut-off valve-branch pipe 28 to divert the product to the jet mixing device (not shown in the drawings).
  • the inlet 22 of the pump 21 is then located as close as possible to the bottom of the tank.
  • the best option for the device is a mechanical heater containing a centrifugal pump 21 with a rotor 24 mounted on the drive shaft 17, since this is the simplest and most durable design.
  • a mechanical heater for the proposed device For the preparation of products requiring additional homogenization (for example, fruit and vegetable juices, mashed potatoes and pastes), the best option for a mechanical heater for the proposed device would be a pumping rotary dispersant, for example, the rotary dispersant according to patent N ° 2156648.
  • the use of a rotary dispersant will allow homogenization simultaneously with heat treatment and reduce the number of stages of the technological process and units of equipment used.
  • the inlet 22 of the pump 21 or dispersant which has the function of a pump, is equipped with a strainer 36 with a suitable cell size, and is mounted on the shaft 17 chopper knife 37.
  • Chopper knife 37 is preferably used in conjunction with a stabilizer 33.
  • the device is used to carry out complex and energy-intensive technological processes, its evaporation circuit is made suitable for incorporating an external heat exchanger, flow heater, or other special-purpose device into it.
  • the device When using the device, its lower part is placed inside the container with the product during its processing, or stationary. In this case, the product level in the tank should be higher than pump 21. Before turning on the device, the processed product through the inlet 22 spontaneously fills the pump housing 23. Further, the device operates as follows.
  • the drive shaft 17 (Fig. 4) is driven by any mechanical or electromechanical drive.
  • the rotor 24 of the centrifugal pump 21 mounted on the shaft 17 and rotating with it rotates the product from the inlet 22 into the outlet pipes 25 and then through the pipelines 27 to the injection device 26 (or devices) and back to the container.
  • the mesh filter 36 if installed, prevents large pieces of product from entering the pump and then into the circuit, and the bearing 35 significantly reduces the radial run-out of the shaft 17, improving the operating conditions of the device.
  • the chopper knife 37 if installed, rotates in close proximity to the strainer 36, preventing it from clogging and the occurrence of hydraulic congestion.
  • the device can be used as part of an evaporation device, to a large extent using mechanical heating of the product.
  • the power of mechanical heating is determined by the diameter of the rotor 24, its rotation frequency, and the effective flow area of the circuit.
  • a control valve 32 of the injector device is used, which allows hydraulically controlling the instantaneous flow rate in the circuit and the heating power.
  • an additional flow heater or a heat exchanger of any design that does not violate the normal circulation mode in the circuit can be placed in the circuit between the pump 21 and the injection device 26 instead of a fragment of the pipeline 27.
  • valve 32 and sensor 31 may not be used when heating the product, but mechanical power control heating, if necessary, vsholnyat by changing the rotor speed.
  • the outputs of the injection devices 26 should be located above the level of the product in the tank.
  • the heated product coming into the tank from the injection device is in a suspended droplet-jet state for some time, which improves the conditions for its evaporation.
  • the injection device When evaporating without boiling the product, it is advisable to make the injection device in the form of a nozzle or sprinkler device, which provides a large free surface of suspended droplets of the product and thereby accelerates the natural evaporation in a dry gas medium.
  • the device When evaporating with boiling of the product, the device allows to realize the volume boiling mode.
  • the injector device 26 is endowed with the function of a hydraulic throttle, that is, it is designed so that the instantaneous flow rate of the product used during evaporation creates a pressure drop across the injector device and an increased pressure inside the circuit.
  • the necessary increased pressure is provided by the pump 21.
  • boiling press the product is heated in the circuit above the boiling temperature in the tank, but the product does not boil inside the circuit due to increased pressure.
  • the pressure in it drops and volume boiling begins due to the internal heat of the product. With this boiling point, the temperature of a portion of the product quickly decreases to the boiling point in the container and its boiling stops.
  • the boiling of the product is preferably carried out in suspension, that is, the boiling time of a portion of the product should not significantly exceed the time it was in suspension. For this, it is necessary to ensure a high boiling speed of the product and a sufficient (usually at least 10 cm) gap between the surface of the product in the container and the outlet of the injection device.
  • the boiling speed of the product can be increased by increasing its overheating relative to the boiling point in the tank.
  • the superheat is measured as the temperature difference measured by the sensor 31 and the sensor 30 or another temperature sensor in the tank.
  • the superheat value is controlled by changing the instantaneous flow in the circuit using the control valve 32.
  • the means for controlling the flow and temperature increment in the circuit can be omitted if the product and its evaporation mode are known and unchanged in advance, and the injection device 26 at a given heating power in the circuit provides sufficient excess pressure and a sufficient increment of the product temperature in it (in practice, 0.2 ° C or more, depending the remainder of the product).
  • the design of the injection device for volume boiling is not critical, since the dispersion of the boiling product is not important.
  • the injection device 26 can be a stationary narrowing diaphragm, i.e. simply narrowed to the desired section output from the evaporation circuit.
  • the operation of the device described above allows heating and evaporation of the product. If instead of the indicated functions or together with them it is necessary to carry out the dispersion and homogenization of the product, in the device As a pump 21, a rotary disperser is used, which performs the functions of a pump and a mechanical heater, if required. If the product contains large and subject to grinding pieces of raw materials, the device is also equipped with a strainer 36 and a chopper knife 37 ( Figure 5). When performing homogenization of the product, the device operates as follows.
  • the product With the dispersing pump 21, the product is sucked into the inlet 22, while large inclusions cannot enter it due to the installed strainer 36 and are excised with the chopper knife 37. So that the mass with lump inclusions does not rotate together with the chopper knife, it is inhibited by the blades 34 of the stabilizer 33.
  • Pre-cut and shredded pieces of raw material are pressed by the product stream to the strainer and are wiped with a rotary chopper.
  • the pulp-like product that passed through the strainer is then subjected to further grinding and homogenization in the disperser 21 with simultaneous mechanical heating, is fed into the outlet pipe 25, and then returned through the pipelines 27 and the injection device 26 to the tank. For high-quality homogenization, this cycle is repeated many times.
  • homogenization at elevated temperature is used, including the simultaneous evaporation of the product, which is performed by the previously described methods.
  • the proposed device (Fig. 4) is widely versatile and can be used for processing and preparing a wide variety of products.
  • the technical result of the invention is that it can be used to heat treat and evaporate any fluid products and mixtures without overheating. If necessary, the device also allows, along with heat treatment, to homogenize the product.
  • Another technical result of the invention is the evaporation of highly viscous fluid products without foaming, obtaining high quality end products and reducing energy consumption.
  • the present invention was used to create cooking-evaporation devices (apparatuses) for cooking various types of caramel “Siberian Burenka” and candy caramel “Dropsi”. According to the conditions for the production of cooking, portions of caramel weighing 50-70 kg should have been carried out in no more than 40 minutes. Evaluation according to formula (2), taking into account the initial recipe and the final moisture of the product, as well as trial cooking of caramel, indicated a minimum heating power of 15 kW. As a heater and a pump in the evaporator circuit, the device depicted in FIG. 4, namely, a submersible centrifugal pump, which was manufactured as part of each cooking-evaporation apparatus.
  • the installed engine power of the device was 17 kW for the Sibirskaya Burenka caramel and 15 kW for the Dropsi candies, with the possibility of obtaining power higher than the rated one due to supplying the engine with an alternating current frequency above 50 hertz.
  • the apparatus for cooking caramel was deprived of the means of mechanical mixing of the mass and equipped with only one high circuit, but to improve the homogeneity of the mass, two injection devices were installed in one circuit, which were located diametrically on the container lid to each other.
  • valves of adjustable output section were used, which, when using a centrifugal pump, made it possible to control the flow rate in a complete circuit, and change the power and amount of heating in the desired direction, i.e. increment of product temperature in the circuit.
  • the operation mode of the evaporator circuit is selected so that it satisfies the condition:
  • Relation (3) shows the relationship between the process parameters and makes it possible to evaluate and correctly select the technical characteristics of the devices used in the cooker to obtain the required heating of the product in the circuit. If we are talking about controlling the actual process of evaporation, then to obtain the desired temperature increment in the circuit, it is no longer necessary to do calculations, especially since the heat capacity of the product may not be known. It is enough to be able to regulate the instantaneous flow rate of the product included in relation (3) and directly measure the temperature increment of the product in the circuit.
  • the process of cooking caramel in the cooker-evaporator according to the claimed method is divided (in the order of execution) into three stages: the heating and mixing stage, where the initial components are introduced and subjected to heating, melting and mixing, the evaporation (boiling) stage and the off-stage the introduction of flavorings and dyes, on which temperature-sensitive components are introduced and mixing is performed without heating and boiling.
  • evaporation begins at a temperature of about 112 ° C.
  • the boiling point may vary depending on the product recipe and deviations in moisture of the components to be laid.
  • the evaporation process is carried out until the product reaches a temperature of 117-118 ° C for Sibirskaya Burenka caramel and 135-137 ° C for Dropsi candy caramel.
  • the difference in the temperatures of the end of evaporation is caused by the recipe difference of different types of sweets, and in the second case, by deviations as a feedstock, in particular molasses, and the possibility of “drying” the mass during subsequent vacuum unloading from the apparatus.
  • the value A which is included in relation (3), is from 0.2 to 0.5 ° C depending on the type of product and the quality of the raw materials used. Accordingly, at the boiling stage of the product, the value of the temperature increment in the circuit is maintained by the operator not lower than the indicated values due to the flow control, while the rest of the time it can be about 0 ° C.
  • the control of the flow rate in the evaporator circuit is already carried out in order to maintain the optimum power of the mechanical heater - pump, since at this stage the density and viscosity of the mass to be processed change significantly.
  • the heater power at the first and second stages of cooking is maintained at a level of 80-100% of the maximum, in order to simultaneously provide sufficient performance and the absence of motor overload.
  • the third stage is performed at a reduced speed due to the reduction of power revolutions for several minutes with visual inspection of the product uniformity, then the product is drained.
  • An example of the implementation of the method may be the concentration (drainage) of glycerol.
  • This product is hygienically safe and is widely used in the chemical and light industries, as well as in the technology and production of cosmetics.
  • glycerin In a concentrated state, glycerin has a boiling point of 290 ° C, that allows you to use it as a harmless and chemically passive coolant for use in a wide temperature range.
  • glycerin is very hygroscopic and is produced in industrial volumes with an admixture of water.
  • Glycerin used as a heat carrier should not boil inside the heat exchange circuit up to the maximum temperature attainable in it under the conditions of use. This, taking into account the pressure available in the circuit, imposes a restriction on the saturated vapor pressure of the polluting solvent, i.e. water, and ultimately the concentration of the pollutant. The higher the temperature of use of the coolant, the cleaner it should be.
  • glycerol is drained by evaporation with boiling in a vacuum tank.
  • the tank is sealed and equipped with a vacuum steam exhaust line with a built-in steam condenser and a serial vacuum pump.
  • the steam condenser is cooled by an external refrigerant with a temperature of preferably about 0 ° C.
  • the required final concentration of water in glycerin is recalculated to the boiling point of the mixture at a pressure in the tank, which is set by the used vacuum pump.
  • the power of the vacuum pump and heater are selected based on the required performance for the finished product, taking into account the ratio (2), the initial humidity of glycerin and its possible deviations.
  • glycerin is not heat-sensitive, therefore, the temperature increment in the complete circuit is limited from above by the technical capabilities of the equipment. In practice, for successful evaporation of liquids of technical purity with volumetric boiling, an increment of 1 ° C or lower is sufficient. In this case, the developer A unit can set this parameter with a value, for example, of 1 ° ⁇ or more, in order to equip the unit with devices coordinated with each other according to technical characteristics.
  • the injection device must satisfy the same principles and, in the specific case, is made in the form of an adjustable or unregulated nozzle.
  • a plate pump with a significant inlet cross section and a low rotor speed is used to supply the product to the evaporator circuit.
  • the pump performance is coordinated with the power of the heater using the relation (3), in which ⁇ is determined empirically, or is taken equal to, for example, 1 ° C or higher, as indicated earlier. Due to the fact that a volumetric principle pump is used, the regulation of the injection device can no longer affect the flow rate in the evaporator circuit and the increment of the product temperature, but can affect the pressure inside the evaporator circuit and the dispersion of the product droplets returned into the tank.
  • the evaporation process is as follows.
  • a portion of the initial glycerin mixture is placed in the capacity of the evaporator. Turns on through the evaporator circuit. The vacuum pump is turned on, and the pressure inside the tank is reduced to the working one. If there is a danger of volume boiling of the mixture in the tank, do not reduce the pressure very quickly. After reaching the working pressure in the tank, heating in the circuit is switched on and evaporation with boiling is performed until the calculated temperature is reached (see above), after which the process is stopped and the glycerin coolant ready for use is discharged. For a stably high quality coolant, it is necessary to stabilize the pressure in the tank at the final stage of the process in each unit evaporation cycle. If this is difficult to achieve, then the evaporation process is carried out to a boiling point higher than the calculated one.
  • Example 3 Evaporation of extracts containing biologically active components. Active substances of biological origin often do not differ in high heat resistance and begin to break down and lose their properties even at temperatures above 30-40 ° ⁇ . And if the extract is aqueous, then it is also subject to the destructive effects of microflora, which develops quite actively at temperatures of 10-40 ° C. The use of the vacuum method of boiling at such temperatures requires a relatively high vacuum and the use of a sufficiently powerful vacuum pump, since as the pressure decreases, the mass capacity of the vacuum pump decreases. Under these conditions, just evaporation with tank ventilation may turn out to be more energy-efficient and technically simple.
  • Evaporation of these extracts by the present method is carried out in an apparatus with a closed tank ventilation circuit, since it is necessary to ensure the proper purity of the product. Since atmospheric oxygen adversely affects the quality of the product, a gas inert to the product, such as nitrogen or carbon dioxide (carbon dioxide), is used to ventilate the tank. Carbon dioxide is also used as a preservative (E290).
  • a gas inert to the product such as nitrogen or carbon dioxide (carbon dioxide)
  • Carbon dioxide is also used as a preservative (E290).
  • the evaporation of aqueous extracts according to the claimed method is carried out in a carbon dioxide atmosphere at atmospheric pressure and a temperature inside the tank of 10-20 ° C.
  • a steam condenser is used, cooled by a coolant with a temperature of preferably 0 ° C, and any hermetically built-in fan corresponding to a given steam output (taking into account its concentration in gas).
  • a droplet eliminator of any suitable design can also be installed in the ventilation circuit at the outlet of the tank.
  • the temperature at the outlet of the complete circuit is limited to 30 ° C, and to exclude the possibility of local overheating, a plate heat exchanger with a coolant temperature of 30 ° C is used as a heater, or an electric heater controlled by a temperature thermostat heating the surface - sti. Since evaporation is carried out without boiling the product, an overpressure in the evaporator circuit under the conditions of heating and evaporation is not required. Therefore, any circulation pump that is satisfactory in performance can be used as a pump, and the pressure drop across the injector device, unlike the previous examples, is no longer necessary. On the other hand, with such evaporation, it is preferable to have a developed free surface and to feed the product in a droplet form.
  • the injector device of the complete circuit in this case is preferably performed in the form of a sprinkler device or nozzle. In the case of using a nozzle, the minimum required differential pressure on it is required for the normal functioning of the device.
  • the time-average power of the heater is selected based on the required capacity for the initial or finished product, taking into account relation (2) and the degree of evaporation, defined as the mass ratio of the initial and finished concentrated extract.
  • relation (1) is not used, and the pump capacity is selected so as to provide the required average power of the heater.
  • the parameters of the heater and pump are selected in concert and jointly.
  • relation (3) in this implementation of the method is also not mandatory, since product boiling and foaming in this case are absent. If the evaporated product admits significant mechanical stresses inside, then the pump and the heater of the complete circuit can be implemented as a mechanical heater according to patent RU 2267350. The task of preventing overheating of the product in this case is easily solved by the method described in the patent description.
  • Evaporation of aqueous or alcoholic extracts with biologically active components using capacity ventilation in the described example is performed as follows.
  • a portion of the feedstock is placed in the tank, after which the ventilation circuit and the space above the product in the tank are filled with an inert gas (nitrogen or carbon dioxide). Then, everything included in the booster apparatus, device is turned on, and the process is carried out until the required degree of evaporation is achieved, i.e. in fact, until the required mass of the product remaining in the tank or obtained in the process of condensation is reached.
  • the inert gas pressure is maintained at atmospheric pressure or slightly higher to prevent air from entering the apparatus due to possible violation of the integrity of the seals.
  • the devices of the evaporator are switched off and the finished product is drained
  • the present invention can be used in chemical, food, processing, medical and other fields where it is necessary to carry out heat treatment and evaporation.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention concerne un procédé d'évaporation de produits en écoulement, qui consiste à mettre en circulation un produit se trouvant dans un récipient (1) et à le chauffer. La circulation du produit se fait via un circuit d'évaporation (2) qui comprend au moins une pompe (3) afin de collecter le produit depuis le récipient (1) et d'assurer sa circulation dans le circuit d'évaporation (2), au moins une unité de chauffage (5) afin de chauffer le produit dans le circuit d'évaporation (2), et au moins un dispositif d'injection (4) pour réinjecter le produit dans le récipient (1) connectés en série par des conduits ; on prélève de manière forcée depuis le récipient (1) dans le circuit d'évaporation (2) une partie du produit que l'on chauffe dans l'unité de chauffage (5) du circuit d'évaporation (2), et le produit chauffé est réinjecté dans la partie supérieure du récipient (1) au-dessus de la surface du produit. L'invention concerne un dispositif d'évaporation destiné à l'évaporation de produits fortement visqueux n'entraînant pas de génération de coûts, et permettant de produire des produits finis de haute qualité avec une diminution des dépenses énergétiques, ainsi qu'n dispositif de traitement thermique et d'évaporation.
PCT/RU2013/000969 2013-10-31 2013-10-31 Procédé d'évaporation de produits en écoulement et dispositif d'évaporation pour sa mise en œuvre WO2015065228A1 (fr)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110508014A (zh) * 2019-08-05 2019-11-29 贵州民族大学 一种提取液浓缩系统

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