RU2344866C1 - Solid-liquid phase extraction unit and solid-liquid phase extraction method - Google Patents

Abstract

FIELD: mechanics.

SUBSTANCE: invention is used for solid-liquid extraction to extract components, extracts, juices from solid-phase materials, low-succulent and succulent vegetable and animal raw materials, hydrobionts, and dispersion fluids and pulps. The unit is comprised of a grinder, infuser, decanting thickener for infused pulp, mixer, shell-and-tube tube-in-tube extractor with convective permeable inner tube and pulse system and decanting thickener for extracted pulp. The extractor shell is separated by longitudinal baffles in even number of channels with extractant inlet nozzles on one end and extractant discharge nozzles on the other end. Pulp is fed into the tube and extractant is fed in counter-flow into the extractor shell channels. The pulse system creates alternating differential pressures between the longitudinal channels of the extractor shell. The infuser and mixer are connected by return pipe to the extract outlet of the extractor shell, and liquid-phase outlet of the extracted pulp decanting thickener is connected to fresh extractant inlet of the extractor. Options for extraction of moderately grindable raw materials, such as drupaceous and seed raw materials and grapes, include auger with rotary drive in the inner tube of the extractor. Solid-liquid phase extraction method includes raw materials grinding and mixing with liquid for fluid pulp formation, counterflow convective mass transfer between pulp and extractant flows in adjacent channels with permeable walls while creating alternating differential pressures between them for repeated transverse liquid-phase exchange to produce extracted pulp and extractant, extracted pulp thickening and return of the liquid phase thus obtained into the process, whereby ground materials are mixed with recirculated extract and liquid phase obtained during extracted pulp thickening is mixed with fresh extractant being fed for extracting. In one of the versions low-succulent raw materials are infused and thickened with a part of the recirculated extract to obtain one product - infused extract, and thickened pulp is mixed with the other part of the extract and fed for extracting. In the second version first product - natural juice is extracted from succulent raw materials and flown down pulp is mixed with a part of extract and fed for extracting to obtain the second product - extract of flown down pulp. Raw materials are ground into dispersion particles of sizes greater than those of perforations in the permeable inner tube being used, within 0.05 to 5.0 mm. Porosity within 0.6 to 0.83 is maintained in the pulp fed to the extractor. Relation between the dose of fresh extractant being used and the volume of processed raw materials is maintained within 0.33 to 1.0.

EFFECT: increased rate of component extraction from raw materials, increased unit capacity for extracted components with reduced number of processing steps and units of equipment to be used.

17 cl, 6 dwg, 1 tbl

Description

The invention relates to techniques and technology for extraction processes in a solid-liquid system and can be used in food, chemical, pharmaceutical, oil, pulp and paper, microbiological, metallurgical, energy and other industries for extracting components from solid-phase, low-fat and juicy raw materials dispersed fluids and pulps.

A known installation for extraction in a solid-liquid system containing a crusher-dosing device, a mixer with an extractant supply pipe, a material pulp supply pump, a thickener-decanter (sedimentation tank, centrifugal separator, filter), a collector, pumps for extracting and condensed extracted pulp [1]. There are only 7 units of equipment in this installation, of which the main volumetric equipment is 3 units.

The disadvantages of the known installation are the low degree of extraction of the component from the material and the low concentration of the obtained extract. And therefore, the specific volumetric capacity of the installation for the recoverable component is also small.

A known installation of extraction in a solid-liquid system containing a metering crusher and three stages of mixing-phase separation connected in series, each of which includes a mixer, material pulp feed pump, thickener-decanter (settler, centrifugal separator, filter), collector and pump pumping of extractant, pipelines and pumps of counterflow pulp and extractant supply between steps, a device for washing and separating thickened extracted pulp [2]. In this installation, only 17 pieces of equipment, of which the main volumetric equipment - 6 units.

The degree of extraction of the component from the material in this installation is higher and the concentration of the resulting extract is greater. But this installation is much more complicated, it has a large number of units and a large amount of equipment used. And therefore, the specific volumetric productivity of the equipment with respect to the recoverable component remains low (less than in a single-stage installation).

Closest to the proposed one is a known installation for phase-selective extraction in a solid-liquid system, containing a dosing crusher, a mixer with a supply pipe for extractant parts, a shell-and-tube extractor, a pipe in a pipe with a convectively permeable inner pipe and a pulsator, a thickener-decanter with the pipeline for the removal of the liquid phase into the mixer, the countercurrent pulp feed pumps from the reactor-mixer into the pipe and the extractant into the casing, recirculation and technological pipelines [3]. In this installation, only 6 units of equipment, the main volumetric equipment - 3 units.

There are relatively few pieces of equipment in this installation. The shell-and-tube pulsating extractor included in its composition with pipes permeable to the liquid phases of the pulp and extractant and impermeable to pulp particles provides the possibility of multiple contact of the particles of the extracted material moving in the pipes as part of the pulp stream with the extractant supplied by the countercurrent to the extractor casing.

The achieved degree of extraction and specific productivity of the equipment here may be higher than in the well-known single-stage unit [1] and comparable with the well-known three-stage unit for mixing-phase separation [2].

But the connection of the mixer with the pipelines for supplying fresh extractant into it with a zero concentration of the component and the liquid phase of the already extracted pulp from the thickener-decanter is the reason for obtaining an insufficiently concentrated extract on the known plant.

The known installation is not equally adapted for optimal processing of the main types of raw materials, differing in moisture or juice content: dry solid phase, low-fat and juicy, and the permissible fineness of its crushing. The pulsation system of the extractor is also not universal enough.

There is a method of extraction in a solid-liquid system, including crushing and mixing solid finely dispersed material with a liquid extractant to obtain pulp, holding it under stirring and thickening by settling or centrifugation, or filtration to obtain an extract and thickened pulp of the extracted material [1]. In this method, 4 technological operations.

An important advantage of this method is that the material is mixed with the extractant in a crushed finely divided state. The intra-diffusion resistance to component transfer in small particles of such a material is small, and the rate of extraction from the particles is quite high.

But, on the other hand, finely dispersed particles are more difficult and longer to separate from the extract, especially by settling from pulp with a small density difference between solid and liquid phases. And the equipment required for this for sedimentation, centrifugation and filtration is cumbersome, complex and energy intensive.

The disadvantages of this method are also the low degree of extraction of the component from the material and the low concentration of the obtained extract. This is due to the fact that only one phase contact step is carried out and the extracted material is removed from the process in the form of its thickened pulp in the extract. The component is lost with both the solid and liquid phases of the discharged condensed pulp. And therefore, the degree of extraction and the specific volumetric productivity of the process for the extracted component is small.

A known method of extraction in a solid-liquid system, comprising crushing and mixing a solid finely divided material with a liquid extractant to obtain pulp and three stages of mixing-separation of phases, each of which includes mixing phases, holding the pulp and thickening it by settling or centrifugation, or filtration, countercurrent pumping of the liquid phase and thickened pulp of the material from step to step, washing and separating the pulp to obtain an extract and extracted material [2]. In this method, 18 technological operations.

The degree of extraction of the component from the material by this method is higher and the concentration of the resulting extract is greater. But according to this method, the number of technological operations and units of equipment used is significantly larger (4.5 times). And less specific volumetric productivity of the process for the extracted component.

Closest to the proposed one is the known method of phase-selective extraction in a solid-liquid system, including crushing the raw material and mixing it with a part of the liquid extractant to obtain a flowing pulp, countercurrent convective mass transfer between pulp and extractant flows in adjacent channels with permeable walls when alternating between them is created pressure drops for multiple transverse (cross) exchange of flows in portions of the liquid phase to obtain extracted pulp and extract, with uschenie extracted pulp and return obtained by this liquid phase for mixing with the crushed raw material [3]. In the method of 6 technological operations.

In the process of countercurrent convective mass transfer of pulp and extractant flows separated by a permeable wall, multiple exchange of liquid phases between these flows is created - inter-channel exchange and exchange of components between material particles and extractant in the pulp - interphase exchange. In this case, the particles of the extracted material do not pass through the permeable wall, do not enter the extractant stream in another channel, and are not removed from the apparatus with the extract. The relative velocity of the counterflow of particles of the extracted material in one channel and the extractant in the other channel here may be greater than in the known processes of continuous countercurrent phases in which small particles are simply carried out of the apparatus with the extractant. And moreover, in this method, the relative countercurrent velocity does not depend on the difference in the densities of the material and the extractant and the particle sizes of the material. This original process of countercurrent extraction of pulp through a convectively permeable wall when creating alternating pressure drops on it, the authors gave the name phase-selective extraction.

The known method is not equally effective in the processing of the main types of raw materials that differ in moisture or juice content: dry solid phase, low-fat and juicy.

When processing dry solid-phase and low-fat raw materials, mixing crushed raw materials with an extractant of zero concentration excludes the possibility of obtaining a high concentration of product extract.

When processing juicy raw materials, mixing crushed raw materials with an extractant irrationally dilutes the high-value natural juice of raw materials.

For the same reason, it is also irrational to return the low-concentrated liquid phase obtained by thickening the extracted pulp to mixing with crushed raw materials.

An object of the invention for the device is to increase the intensity of inter-channel and interphase mass transfer in the extractor, the efficiency of the pulsation system, the compactness of the equipment and the stability of its operation, providing the possibility of optimal processing of the main types of raw materials, increasing the concentration of the extract, the degree of extraction and the specific volumetric productivity of the equipment for the extracted component.

This goal is achieved by the fact that in the known installation for phase-selective extraction in the system, a solid body is a liquid containing a crusher connected in series, a mixer with a liquid supply pipe, a shell-and-tube extractor, a pipe in a pipe with a convective-permeable inner pipe, a thickener-decanter of the extracted pulp with a pipeline for removing the liquid phase from it, pumps for countercurrent pulp supply from the mixer to the pipe and extractant to the casing, recirculation and process pipelines, cm the carrier is connected by a pipeline to the outlet of the extract from the casing of the extractor, the pipeline for removing the liquid phase from the thickener-decanter of the extracted pulp is connected to the input of the extractant into the extractor, the casing of the extractor is divided by longitudinal partitions into an even number of channels with extractant inlets, nozzles and an extract pump for pumping them The installation is also equipped with a pulsation system, including valves on these nozzles and a control computer, which ensures their cross opening and closing. In this installation, only 9 units of equipment, the main volumetric equipment - 5 units.

In embodiments, the installation is equipped with a thickener-decanter pulp installed between the crusher and the mixer.

In embodiments, the installation is equipped with a tincture installed between the crusher and the mixer.

In embodiments, the tincture is made in the form of a vertical or horizontal cylindrical sectioned apparatus with mixers in sections and a thermostatic jacket on the body.

In embodiments, the tincture is connected by a pipeline to the outlet of the extract from the casing of the extractor.

In embodiments, a hammer mill, or a roller mill, or a disk mill, or a millstone, or a grain mill, or a sugar beet grinder, or a comb mill, or a malt grinder, are used as crushers.

In embodiments, a hydrocyclone, or a reversible filter, or a centrifugal separator, or a stacker, or a screw press, or a settler are used as a thickener-decanter.

In embodiments, the convective-permeable inner tube of the extractor is made of perforated or porous metal, plastic, ceramic, cermet or reinforced composite material.

In embodiments, the convective-permeable inner tube of the extractor is made with holes in the range of 0.03-1.0 mm.

In embodiments, a screw device with a rotation drive is installed in the inner tube of the extractor.

The specified set of features for the device is essentially new and ensures the achievement of the goal.

An object of the invention according to the method is to optimize the parameters of the phase-selective extraction of solid-phase, low-fat and juicy raw materials to obtain one product - extract, to obtain two products: natural juice and extract, as well as products insisted on the feedstock, increase the concentration of products, the degree of extraction of the component from raw materials and specific productivity of the extracted component.

This goal is achieved by the fact that in the known method of phase-selective extraction in a solid-liquid system, including crushing the raw material, mixing it with a liquid to produce a flowing pulp, countercurrent convective mass transfer between pulp and extractant flows in adjacent channels with permeable walls when alternating between them is created pressure drops for multiple transverse exchange of flows in portions of the liquid phase to obtain extracted pulp and extract, thickening the extracted pulp and the return of the obtained liquid phase into the process, crushed raw materials are mixed with the recirculated extract, and the liquid phase obtained by thickening the extracted pulp is mixed with the fresh extractant supplied for extraction.

In embodiments, the crushed juicy raw material is concentrated with the selection of the first product - natural juice, and the top pulp is mixed with a part of the extract and sent for extraction to obtain a second product - extract.

In embodiments, the crushed low-fat raw material is mixed with a portion of the extract, infused and concentrated to obtain a product infused extract, and the thickened pulp is mixed with the rest of the extract and sent for extraction.

In options, crushed juicy raw materials are infused and concentrated with the selection of the first product - infused natural juice, and the top pulp is mixed with a portion of the extract and sent for extraction to obtain a second product - extract.

In options, the raw materials are crushed to the size of dispersed particles larger than the size of the perforations in the used permeable baffle of the extractor, in the range of 0.05-5.0 mm.

In embodiments, the feed supplied to the extractor pulp supports porosity in the range of 0.6-0.83.

In embodiments, the relative dose of fresh extractant used to the volume of processed raw materials is maintained within the range of 0.33-1.0.

The specified set of features by the method is essentially new and ensures the achievement of the goal.

Figure 1 shows the installation for phase-selective extraction of solid-phase and low-fat raw materials to obtain the 1st product - extract, figure 2 - cross section of the extractor, figure 3 - version of the extractor with a screw device in the inner tube for phase-selective extraction of moderately crushed juice-containing 4, a variant of the installation for phase-selective extraction of low-fat raw materials to obtain the 1st product — extract extracted from the feedstock, and FIG. 5 — an installation option for phase-selective extra suction of raw materials with obtaining 2 products: infused natural juice and extract, Fig.6 is a variant of the installation for phase-selective extraction of juicy raw materials with obtaining 2 products: natural juice-gravity juice and extract.

Raw materials are classified as solid-phase, upon crushing of which no liquid phase is released. From food raw materials, this can include grain, malt, beans, seeds, seeds, etc. The porosity of such raw materials is e <0.4.

Juice-containing raw materials are classified as low-fat, when crushed, a liquid phase is released, but the resulting pulp is not sufficiently fluid. From food raw materials, one can include pome fruits, root crops, etc. The porosity of such raw materials is e = 0.4-0.6.

Juice-containing raw materials are classified as juicy, upon crushing of which a liquid phase is formed with the formation of a flowing pulp. From food raw materials, grapes, berries, stone fruits, tomatoes, etc. can be attributed here. The porosity of such raw materials is e> 0.6.

Juice-containing raw materials containing solids not subject to grinding are classified as moderately crushed. From food raw materials, this can include stone fruits, pome fruits, grapes, tomatoes, etc.

The installation in the variant for phase-selective extraction of solid-phase and low-fat raw materials to obtain the 1st product - extract (see Fig. 1) contains series-connected crusher-dosing raw material 1, mixer 2 with a pipe for supplying part of the recirculated extract to it, a shell-and-tube extractor of type 3 a pipe in a pipe with a pulsation system 4 (conditionally), a thickener-decanter of the extracted pulp 5, a pump 6 for feeding the pulp from the mixer into the permeable pipe 8 of the extractor, and a pump 7 for pumping the extracted pulp from it into gustitel-decanter 5. extractant feed line to the extractor pump 9 is mounted.

The shell-and-tube extractor 3 (see FIGS. 1 and 2) is made in the form of an impermeable casing 10, inside of which there is a permeable pipe 8. It can also have an impermeable shirt (not shown) on the casing connected to the supply and exhaust pipelines of the thermostatic agent. The inner tube 8 of the shell-and-tube extractor is made permeable to the continuous liquid phases of the pulp and extractant and impermeable to their dispersed particles. Therefore, it is called convective-permeable. It, depending on the type of pulp being processed and the requirements for the dispersed composition of the extract, is made of perforated or porous metal, plastic, ceramic, cermet or reinforced composite material with a hole size in the range of 0.03-1.0 mm.

The annular space of the shell-and-tube extractor 3 is divided by a longitudinal partition into an even number of channels. Figures 1 and 2 show a variant with separation of the annulus 11 by two channels 12 and 13 with inlet and outlet pipes at the ends and controlled valves 14 and 15 on the extractant supply line 9, 16 and 17 on the extract discharge line.

The pulsation system 4 of the extractor includes the above-mentioned valves 14-17 with pneumatic actuators and a common control unit with a computer. System 4 creates alternating pressure drops between the annulus 12 and 13 of the extractor, where the extractant moves.

In the embodiment of the extractor 3 for phase-selective extraction of moderately crushed raw materials (see figure 3) in the permeable pipe 8 of the extractor is placed a screw device with a rotation drive 18.

The pump 9 for supplying the extractant to the extractor 3 is connected at the inlet with a supply of fresh extractant 19 and a pipe 20 for recirculating the liquid phase from the thickener-decanter 5. The pipe 22 for extracting the extract from the extractor is divided into a recirculation line 23 and part of the extract to the mixer and a product extract line 24.

The installation (see FIG. 4) in the embodiment for phase-selective extraction of low-fat raw materials to obtain the 1st product — extract extracted from the feedstock differs from the installation in FIG. 1 in that it additionally contains a pulp infuser 28 and a thickener-decanter installed after the crusher 1 25. Moreover, the tincture is connected by a pipe 24 for supplying extract from the extractor 3 and is also connected by a pipe 29 and a pump 30 with a thickener-decanter 25.

The installation (see Fig. 5) in the embodiment for phase-selective extraction of juicy raw materials to obtain 2 products: infused natural juice and extract differs from the installation in Fig. 1 in that it additionally contains a pulp infuser 28 and a thickener-decanter installed after the crusher 1 25. Moreover, the tincture is connected by a pipe 29 and a pump 30 with a thickener-decanter 25.

The installation (see FIG. 6) in the embodiment for phase-selective extraction of juicy raw materials to obtain 2 products: natural gravity juice and extract differs from the installation in FIG. 1 in that it further comprises a thickener-decanter 25 installed after the crusher 1, connected mezgoprovod 27 with a mixer 2.

The connection of the mixer by the pipeline with the outlet of the extract from the casing of the extractor provides the technical ability to maintain the porosity of the pulp of crushed raw materials at the level necessary for its fluidity without reducing the concentration of the extracted component in it.

The connection of the pipeline for the removal of the liquid phase from the thickener-decanter of the extracted pulp not with a mixer, as in the prototype, but with the fresh extractant entering the extractor eliminates the technical reason for the decrease in the concentration of the component in the pulp at the inlet of the extractor and the concentration of the extract obtained at its outlet.

Separation of the extractor casing by longitudinal partitions into an even number of channels with extractant supply pipes, extract pump nozzles from them and computer-controlled valves installed on these pipes provide the technical possibility of intensifying inter-channel convective mass transfer by creating alternating transverse flows of extractant from one casing channel through the pulp into the permeable pipe into the second channel of the casing and vice versa. Thus, the intensification of interphase mass transfer between the particles of raw materials moving with the pulp in the pipe and the extractant moving in the channels of the casing is also provided. And this is achieved in the absence of a negative effect of back mixing in the streams.

The supply of the plant with a thickener-decanter of pulp, installed between the crusher and the mixer, gives a technical opportunity when processing juicy raw materials in addition to the extract to receive a certain amount of high-quality gravity wort - natural juice.

Providing the installation with a tincture installed between the crusher and the mixer provides a technical opportunity to process highly extractable infused natural juice during processing of juicy raw materials, and a more concentrated extract infused to the feedstock during processing of raw materials.

The implementation of the tincture in the form of a vertical or horizontal cylindrical sectioned apparatus with mixers in sections and a thermostatic jacket on the body reduces back mixing, eliminates the exit from the apparatus of a part of the infused pulp of raw materials and thus increases the efficiency of the infusion process.

The connection of the tincture with a pipeline with the outlet of the extract from the casing of the extractor provides the technical ability to maintain the porosity of the pulp of crushed raw materials at the level necessary for its fluidity, and to obtain an infused more concentrated extract.

Using as a crusher a hammer crusher, or roller, or disk, or millstone, or grain grinder, or beet slicer-crusher, or crusher-comb separator, or malt crusher, it is possible to ensure optimal grinding, particle sizes of various types of extracted raw materials.

The use of a hydrocyclone as a thickener-decanter, or a reversible filter, or a centrifugal separator, or a stacker, or a screw press, or a settling tank allows for optimal separation, the porosity of various types of extracted raw materials.

The placement of a screw device with a rotation drive in the inner tube of the extractor facilitates the transportation of moderately crushed raw materials containing inclusions, seeds or seeds that cannot be crushed.

The implementation of the convective-permeable inner tube of the extractor from perforated or porous metal, plastic, ceramics, cermets or reinforced composite material allows you to expand the range of used permeable materials.

The implementation of the convectively permeable inner tube of the extractor with the hole size in the range of 0.03-1.0 mm makes it possible to obtain an extract of the required transparency depending on the type of extracted raw material and the requirements for the dispersed composition of the extract.

The mixing of crushed raw materials with the recirculated extract provided for by the method, and obtained by thickening the extracted pulp of the liquid phase with fresh extractant supplied for extraction allows increasing the concentration of the obtained product extract without reducing the degree of extraction of the component from the raw material.

The thickening of crushed raw materials with the selection of the first product - natural juice, mixing the pulp with a portion of the extract and directing it to extraction to obtain a second product - extract infused with a glass pulp allows the rational processing of juicy raw materials.

Mixing crushed raw materials with part of the extract, infusion and thickening to obtain a product infused extract, mixing condensed pulp with the rest of the extract and directing it to extraction allows rational processing of low-fat raw materials.

Insisting crushed raw materials and thickening them with the selection of the first product - infused natural juice, mixing the pulp with a portion of the extract and directing to extraction to obtain a second product - extract allows you to rationally process juicy raw materials to obtain more extractive products.

Crushing of the raw material to the size of dispersed particles in the range of 0.05-5.0 mm, not less than the size of the perforations in the used permeable baffle of the extractor, allows for a sufficiently high rate of inter-channel and interphase mass transfer in the extractor and obtaining an extract with a given dispersed composition.

Maintaining porosity in the raw material supplied to the extractor pulp in the range of 0.6-0.83 allows to ensure its fluidity and stable operation of the extractor on various types of raw materials.

Maintaining the relative dose of fresh extractant used to the volume of processed raw materials in the range of 0.33-1.0 allows us to provide fairly high values of the concentration of the extract and the degree of extraction of the component at moderate costs of fresh extractant.

The installation works and the method is as follows.

Example 1. Phase-selective extraction of solid-phase raw materials of flax seeds with water to obtain the 1st product - protein-lipid dispersion.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . Flax seeds and the resulting whole flaxseed pulp with a flow rate of 1 m ³ / h, a solids concentration of 100 kg / m ³ , a particle size of 0.05-0.6 mm and a porosity of 0.4 are fed into the mixer in a mill mill 1 continuously and grinded 2. In the mixer 2 through the recirculation line 23 continuously with a flow rate of 1 m ³ / h serves part of the extract obtained in the extractor 3 with a solids content of 90 kg / m ³ .

The mixture of whole flaxseed pulp and liquid extract in the mixer 2 is heated at a temperature of up to 87 ° C and kept under stirring for up to 1 hour.

Obtained in the mixer 2 flaxseed pulp with a porosity of 0.7 is supplied by pump 6 with a flow rate of 2 m ³ / h to the inner tube 8 of the extractor 3. A countercurrent pump 9 is fed into the casing 10 of the extractor with fresh extractant - water with a flow rate of 1 m ³ / h plus liquid phase 1 m ³ / h from the extracted pulp concentrated in the thickener-decanter 5. The relative dose of fresh extractant 1. Total consumption of extractant supplied to the casing of the extractor, 2 m ³ / h

Using the computer of the pulsation system 4, the program of valves 14-17 is set, which ensures in the extractor 3 a convective inter-channel mass transfer of flax pulp and extractant flows under the condition t ₁ = t ₂ , where: t ₁ is the tact time of the alternating pressure drop, in which the pressure in channel 12 of the casing of the extractor 3 is larger than in channel 13 of the casing of the extractor; t ₂ is the tact time of an alternating pressure drop in which the pressure in channel 13 exceeds the pressure in channel 12. In this case, alternating transverse flows of extractant are created, passing in the first cycle from channel 12 to the inner permeable pipe 8 and from it to channel 13 (valves 14 and 17 are open, and 15 and 16 are closed), and in the second cycle, in the opposite direction from channel 13 to the inner pipe 8 and from it to channel 12 (valves 15 and 16 are open, and 14 and 17 are closed). These alternating flows penetrate the extracted pulp of raw materials moving in the inner pipe and create a multiple exchange of liquid phases between countercurrent flows of extractant in the channels of the casing and pulp in the permeable pipe. At the same time, during the residence of the pulp and extractant streams in the extractor, multiple countercurrent contact of the extractant with flaxseed pulp particles is carried out, the permeable wall of the inner tube of the extractor is regenerated, the relative speed of the extractant flowing around the raw material particles in the pulp and the rate of extraction of dry matter components from them increase.

Thus, an intense interchannel convective mass transfer is created - between the countercurrent flows of the raw material pulp countercurrent flows in the inner tube 8 and the extractant in the casing channels 12 and 13. Interphase mass transfer is also intensified - between the raw material particles and the extractant liquid phase in the pulp stream itself pipe 8.

On line 24 from the casing 10 of the extractor 3 discharge product water extract flax protein-lipid dispersion with a flow rate of 1 m ³ / h and with a solids content of 90 kg / m ³ . The extracted pulp with a flow rate of 2 m ³ / h and a porosity of 0.7 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a centrifugal separator, where it is divided into phases. Extracted condensed flaxseed pulp - Okara with a flow rate of 1 m ³ / h, solids content of 10 kg / m ³ and a porosity of 0.4 is removed from the thickener-decanter 5. And the liquid phase with a flow rate of 1 m ³ / h through line 20 is returned to be mixed with the pump 9 fed into the extractor 3 with fresh extractant 19. Moreover, the degree of phase-selective extraction of the component from the feedstock is 0.9. The specific volumetric productivity of the extracted component is 30 kg / (h · m ³ ). For the well-known 3-stage mixing-phase separation process with 6 units of equipment with a volume of 6 m ^3, these values are: 0.75 and 12.5 kg / (h · m ³ ).

Example 2. Phase-selective extraction of solid-phase raw materials of soybeans with water to obtain the 1st product - protein-lipid dispersion.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . The beans of pre-soaked soybeans and the resulting whole soybean pulp with a flow rate of 1 m ³ / h, a solids concentration of 120 kg / m ³ , a particle size of 0.05-1.5 mm and a porosity of 0.4 are fed into the hammer mill 1 and continuously ground in the mixer 2. In the mixer 2 through the recirculation line 23 continuously with a flow rate of 1.5 m ³ / h serves part of the extract obtained in the extractor 3 with a solids content of 88 kg / m ³ . The mixture of soybean pulp and liquid extract in the mixer 2 is heated at a temperature of up to 90 ° C and kept under stirring for up to 1 hour.

The soybean pulp obtained in mixer 2 with a porosity of 0.6 is pumped 6 with a flow rate of 2.5 m ³ / h into the inner tube 8 of the extractor 3. A countercurrent pump 9 is fed into the casing 10 of the extractor with fresh extractant - water with a flow rate of 1 m ³ / h plus a liquid phase with a flow rate of 1.5 m ³ / h from the extracted pulp concentrated in the thickener-decanter 5. The relative dose of fresh extractant 1. Total consumption of extractant supplied to the casing of the extractor, 2.5 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

On line 24 from the casing 10 of the extractor 3 discharge product extract - water extract - soy protein-lipid dispersion with a flow rate of 1 m ³ / h and with a solids content of 88 kg / m ³ . The extracted pulp with a flow rate of 2.5 m ³ / h and a porosity of 0.6 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which uses a hydrocyclone, where it is divided into phases. From the thickener-decanter 5, the extracted condensed soybean pulp is removed - okara with a flow rate of 1 m ³ / h, solids content of 12 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 1.5 m ³ / h through line 20 is returned to mixing with the pump 9 fed into the extractor 3 with fresh extractant 1 m ³ / h. The degree of phase-selective extraction of the component from raw materials is 0.9. The specific volumetric productivity of the extracted component is 36 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 15 kg / (h · m ³ ).

Example 3. Phase-selective extraction of solid-phase raw material of chickpea beans with water to obtain the 1st product - protein-lipid dispersion.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . The beans of pre-soaked chickpea and the resulting whole chickpea pulp with a flow rate of 1 m ³ / h, a solids concentration of 110 kg / m, a particle size of 0.05-0.5 mm and a porosity of 0.4 are fed into the disk mill 1 continuously and grinded mixer 2. Into mixer 2, a part of the extract obtained in extractor 3 with a solids content of 99 kg / m is fed continuously through a recirculation line 23 at a flow rate of 1 m ³ / h. The mixture of chickpea pulp and liquid extract in the mixer 2 is heated at a temperature of up to 90 ° C and kept under stirring for up to 1 hour.

Obtained in mixer 2, chickpea pulp with a porosity of 0.7 is pumped 6 with a flow rate of 2 m ³ / h into the inner tube 8 of the extractor 3. A countercurrent pump 9 is fed into the casing 10 of the extractor with fresh extractant - water with a flow rate of 1 m ³ / h plus liquid phase with a flow rate of 1 m ³ / h from the extracted pulp concentrated in the thickener-decanter 5. The relative dose of fresh extractant 1. Total consumption of extractant supplied to the casing of the extractor, 2 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

On line 24 from the casing 10 of the extractor 3 discharge product extract of chickpea protein-lipid dispersion with a flow rate of 1 m ³ / h and with a solids content of 99 kg / m ³ . The extracted pulp with a flow rate of 2 m ³ / h and a porosity of 0.7 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a centrifugal separator, where it is divided into phases. Extracted condensed chickpeas pulp - Okara with a flow rate of 1 m ³ / h, solids content of 11 kg / m ³ and a porosity of 0.4 is removed from the thickener-decanter 5. And the liquid phase with a flow rate of 1 m ³ / h through line 20 is returned to mixing with the pump 9 fed into the extractor 3 with fresh extractant 1 m ³ / h. The degree of phase-selective extraction of the component from raw materials is 0.9. The specific volumetric productivity of the extracted component is 33 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 13.8 kg / (h · m ³ ).

Example 4. Phase-selective extraction of solid-phase raw materials of lentil beans with water to obtain the 1st product - protein-carbohydrate dispersion.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . Beans of pre-soaked lentils and the resulting whole lentil pulp with a flow rate of 1 m ³ / h, a solids concentration of 115 kg / m ³ , a particle size of 0.05-0.2 mm and a porosity of 0.5 are fed into the grain mill 1 continuously and ground mixer 2. Into mixer 2 through a recirculation line 23 continuously with a flow rate of 0.67 m ³ / h, a part of the extract obtained in extractor 3 with a solids content of 104 kg / m ^{3 is} fed. A mixture of lentil pulp and liquid extract in the mixer 2 is maintained at a temperature of up to 70 ° C with stirring for up to 1 hour.

Obtained in the mixer 2 lentil pulp with a porosity of 0.7 is fed by pump 6 with a flow rate of 1.67 m ³ / h into the inner tube 8 of the extractor 3.

A countercurrent pump 9 feeds a fresh extractant into the casing 10 of the extractor — water with a flow rate of 0.67 m ³ / h and a concentration of ammonium sulfate up to 5% plus a liquid phase with a flow rate of 0.67 m ³ / h from the extracted in the thickener-decanter 5 pulp. The relative dose of fresh extractant is 0.67. Total consumption of extractant supplied to the casing of the extractor, 1,67 m ³ / h

The operation of the extractor 3 is carried out, as in example 1. On line 24 from the casing 10 of the extractor 3 discharge product extract - lentil protein-carbohydrate dispersion with a flow rate of 1 m ³ / h and with a solids content of 104 kg / m The extracted pulp with a flow rate of 1.67 m ³ / h and a porosity of 0.7 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a centrifugal separator, where it is divided into phases. From the thickener-decanter 5, the extracted condensed lentil pulp is removed - Okara with a flow rate of 0.83 m ³ / h, a solids content of 13 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 0.84 m ³ / h through line 20 is returned to mix with the pump 9 fed into the extractor 3 with a fresh extractant of 0.83 m ³ / h. The degree of phase-selective extraction of the component from raw materials is 0.9. The specific volumetric productivity of the extracted component is 34.5 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 14.4 kg / (h · m ³ ).

Example 5. Phase-selective extraction of solid-phase raw materials of oilseeds with gasoline to obtain the 1st product of miscella extract.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . A hammer crusher-dispenser 1 is continuously supplied with a consumption of 1 m ³ / h to the mixer 2 oil-seed grits with an oil concentration of 320 kg / m ³ , a particle size of 0.05-1.5 mm and a porosity of 0.4. A portion of the extract obtained in extractor 3 with an oil content of 302 kg / m ^{3 is} fed to the mixer 2 through a recirculation line 23 continuously with a flow rate of 1 m ³ / h. The mixture of grains and liquid extract in the mixer 2 is heated at a temperature of up to 60 ° C and kept under stirring for up to 1 hour.

The oil-seed pulp obtained in mixer 2 with a porosity of 0.7 is supplied by pump 6 with a flow rate of 2 m ³ / h to the inner tube 8 of the extractor 3. A countercurrent pump 9 is fed into the casing 10 of the extractor with fresh extractant gasoline with a flow rate of 1 m ³ / h plus liquid phase with a flow rate of 1 m ³ / h from the extracted pulp concentrated in the thickener-decanter 5. The relative dose of fresh extractant 1. Total consumption of extractant supplied to the casing of the extractor, 2 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

On line 24 from the casing 10 of the extractor 3 discharge product extract miscella with a flow rate of 1 m ³ / h and with an oil content of 302 kg / m ³ . The extracted pulp with a flow rate of 2 m ³ / h and a porosity of 0.7 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which uses a hydrocyclone, where it is divided into phases. From the thickener-decanter 5, the extracted condensed oil-seed pulp is removed - meal with a flow rate of 1 m ³ / h, an oil content of 17.5 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 1 m ³ / h through line 20 is returned to mixing with the pump 9 fed into the extractor 3 with fresh extractant 1 m ³ / h. Moreover, the degree of phase-selective extraction of the component from the feed is 0.94. The specific volumetric productivity of the extracted component is 100 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 40 kg / (h · m ³ ).

Example 6. Phase-selective extraction of low-fat raw material of saccharified grain mash to obtain the 1st product - grain wort in the production of alcohol.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . Dispenser 1 continuously with a flow rate of 1 m ³ / h, a concentration of solids of 160 kg / m ³ , a particle size of 0.05-1.0 mm and a porosity of 0.5 serves sugared cereal mash in mixer 2. Into mixer 2 through recirculation line 23 continuously with a flow rate of 0.25 m ³ / h serves part of the extract obtained in the extractor 3 with a solids content of 142 kg / m ³ . The mixture of cereal mash and extract in the mixer 2 is maintained at a temperature of up to 60 ° C with stirring for up to 1 hour.

The mash pulp obtained in mixer 2 with a porosity of 0.6 is supplied by pump 6 with a flow rate of 1.25 m ³ / h to the inner tube 8 of the extractor 3. By a countercurrent flow to it by pump 9, fresh extractant is fed into the casing 10 of the extractor — water with a flow rate of 0.83 m ³ / h plus the liquid phase with a flow rate of 0.42 m ³ / h from the extracted pulp concentrated in the thickener-decanter 5. The relative dose of fresh extractant 0.83. Total consumption of extractant supplied to the casing of the extractor, 1.25 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

On line 24 from the casing 10 of the extractor 3 discharge product grain extract with a flow rate of 1 m ³ / h and with a solids content of 142 kg / m ³ . The extracted pulp with a flow rate of 1.25 m ³ / h and a porosity of 0.6 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a hydrocyclone, where it is divided into phases. From the thickener-decanter 5, the extracted pellet is withdrawn with a flow rate of 0.83 m ³ / h, a solids content of 22 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 0.42 m ³ / h through line 20 is returned to mix with the pump 9 fed into the extractor 3 with a fresh extractant of 0.83 m ³ / h. The degree of phase-selective extraction of solids from raw materials of 0.89. The specific volumetric capacity for extracted solids is 47.5 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 20 kg / (h · m ³ ).

Example 7. Phase-selective extraction of low-fat malt mash raw materials to obtain the 1st product - malt extract in beer production.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . A batcher 1 continuously with a flow rate of 1 m ³ / h, a concentration of solids of 150 kg / m ³ , a particle size of 0.05-1.0 mm and a porosity of 0.6 serves a malt mash in the mixer 2. In the mixer 2 through the recirculation line 23 continuously with a flow rate of 0.33 m ³ / h serves part of the extract obtained in the extractor 3 with a solids content of 137 kg / m ³ . The mixture of malt mash and extract in the mixer 2 is kept at a temperature of up to 75 ° C with stirring for up to 1 hour.

The malt pulp obtained in mixer 2 with a porosity of 0.7 is supplied by pump 6 with a flow rate of 1.33 m ³ / h to the inner tube 8 of the extractor 3. By a countercurrent flow to it by pump 9, fresh extractant is fed into the casing 10 of the extractor — water with a flow rate of 0.69 m ³ / h plus the liquid phase with a flow rate of 0.64 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant is 0.69. Total consumption of extractant supplied to the casing of the extractor is equal to 1.33 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

On line 24 from the casing 10 of the extractor 3 discharge product malt extract with a flow rate of 1 m ³ / h and with a solids content of 137 kg / m ³ . The extracted pulp with a flow rate of 1.33 m ³ / h and a porosity of 0.7 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a centrifugal separator, where it is divided into phases. An extracted pellet is withdrawn from the thickener-decanter 5 with a flow rate of 0.69 m ³ / h, a solids content of 19 kg / m ³ and a porosity of 0.42. And the liquid phase with a flow rate of 0.64 m ³ / h through line 20 is returned to mix with the pump 9 fed into the extractor 3 with a fresh extractant of 0.69 m ³ / h. Moreover, the degree of phase-selective extraction of the component from raw materials is 0.91. The specific volumetric productivity of extracted solids is 45.5 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 18.8 kg / (h · m ³ ).

Example 8. Phase-selective extraction of low-fat raw materials of sugar beet root crops with water to obtain the 1st product - beetroot extract.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . Beets and the whole beet pulp obtained at 1 m ³ / h, a sugar concentration of 180 kg / m ³ , a particle size of 0.05-5 mm and a porosity of 0.5 are fed into mixer 2 in a beet grinder 1 continuously and chopped the mixer 2 through a recirculation line 23 continuously with a flow rate of 0.25 m ³ / h serves part of the extract obtained in the extractor 3 with a sugar content of 168 kg / m ³ . The mixture of whole beet pulp and extract in the mixer 2 is kept at a temperature of up to 80 ° C with stirring for up to 1 hour.

The beet pulp obtained in mixer 2, with a porosity of 0.6, is pumped 6 with a flow rate of 1.25 m ³ / h into the inner tube 8 of the extractor 3. By a countercurrent flow to it, pump 9 supplies fresh extractant to the extractor casing 10 — fresh water with a flow rate of 0.83 m ³ / h plus the liquid phase with a flow rate of 0.42 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant 0.83. Total consumption of extractant supplied to the casing of the extractor, 1.25 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

On line 24 from the casing 10 of the extractor 3 discharge beetroot extract with a flow rate of 1 m ³ / h and sugar content of 168 kg / m ³ . The extracted pulp with a flow rate of 1.25 m ³ / h and a porosity of 0.6 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a screw press, where it is divided into phases. Extracted pulp is removed from the thickener-decanter 5 with a flow rate of 0.83 m ³ / h, a sugar content of 15 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 0.42 m ³ / h through line 20 is returned to mix with the pump 9 fed into the extractor 3 with a fresh extractant of 0.83 m ³ / h. The degree of phase-selective extraction of sugar from raw materials is 0.93. The specific volumetric productivity of extracted sugar is 56 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 22.5 kg / (h · m ³ ).

Example 9. Phase-selective extraction of low-fat raw fruits of apples with water to obtain the 1st product - apple extract.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . In the hammer mill 1, the fruits of apples and the whole apple pulp obtained are continuously fed and crushed with a flow rate of 1 m ³ / h, a sugar concentration of 140 kg / m ³ , a particle size of 0.1-5 mm and a porosity of 0.5 are fed into mixer 2. B the mixer 2 through the recirculation line 23 continuously with a flow rate of 0.25 m ³ / h serves part of the extract obtained in the extractor 3 with a sugar content of 124 kg / m ³ . The mixture of whole apple pulp and extract in the mixer 2 is kept at a temperature of up to 80 ° C with stirring for up to 1 hour.

The apple pulp obtained in mixer 2 with a porosity of 0.6 is pumped 6 with a flow rate of 1.25 m ³ / h into the inner tube 8 of the extractor 3. A countercurrent pump 9 is fed into the extractor casing 10 — fresh water with a flow rate of 0.91 m ³ / h plus the liquid phase with a flow rate of 0.34 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant is 0.91. Total consumption of extractant supplied to the casing of the extractor, 1.25 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

On line 24 from the casing 10 of the extractor 3 discharge product extract - apple juice with a flow rate of 1 m ³ / h and a sugar content of 124 kg / m ³ . The extracted pulp with a flow rate of 1.25 m ³ / h and a porosity of 0.6 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a screw press, where it is divided into phases. Extracted pulp is removed from the thickener-decanter 5 with a flow rate of 0.91 m ³ / h, a sugar content of 18 kg / m ³ and a porosity of 0.45. And the liquid phase with a flow rate of P ₅ = 0.34 m ² / h along line 20 is returned to mixing with the pump 9 supplied to the extractor 3 with a fresh extractant of 0.91 m ³ / h. The degree of phase-selective extraction of the component from raw materials is 0.89. The specific volumetric capacity for extracted sugar is 41.5 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 17.5 kg / (h · m ³ ).

Example 10. Phase-selective extraction of low-fat raw materials of sweet fruit-bearing sediments with water to obtain the 1st product - fruit-fruit extract in the production of juices and drinks.

According to this example, the process is carried out in the installation of figure 1 with a total volume of basic equipment of 3 m ³ . Dispenser 1 continuously serves sweet fruiting with a flow rate of 1 m ³ / h, solids concentration c ₁ = 130 kg / m ³ , particle size 0.1-1.3 mm and a porosity of 0.5 to mixer 2. Into mixer 2 recirculation line 23 continuously with a flow rate of 0.25 m ³ / h serves part of the extract obtained in the extractor 3 with a solids content of 116 kg / m ³ . The mixture of precipitation and extract in the mixer 2 is maintained at a temperature of up to 20 ° C with stirring for up to 1 hour.

The fruit-bearing pulp obtained in mixer 2 with a porosity of 0.6 is supplied by pump 6 with a flow rate of 1.25 m ³ / h to the inner tube 8 of the extractor 3. A countercurrent pump 9 is fed into the casing 10 of the extractor with fresh extractant - water with a flow rate of 0.83 m ³ / h plus the liquid phase with a flow rate of 0.42 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant 0.83. Total consumption of extractant supplied to the casing of the extractor, 1.25 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

On line 24 from the casing 10 of the extractor 3 discharge fruit-bearing fruit extract with a flow rate of 1 m ³ / h and with a solids content of 118 kg / m ³ . The extracted pulp with a flow rate of 1.25 m ³ / h and a porosity of 0.6 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a settler, where it is divided into phases. Extracted sediments are withdrawn from the thickener-decanter 5 with a flow rate of 0.83 m ³ / h, a solids content of 15 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 0.42 m ³ / h through line 20 is returned to mix with the pump 9 fed into the extractor 3 with a fresh extractant of 0.83 m ³ / h. Moreover, the degree of phase-selective extraction of solids from raw materials 0.91. The specific volumetric productivity of extracted solids is 39.3 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 16.3 kg / (h · m ³ ).

Thus, from the sweet fruit-bearing sediments of the production of juices and drinks, which are difficult to separate because of the small difference in the density of the pulp and wort particles, according to this invention, extractor 3 produces a product sweet extract and well-separated unsweetened pulp even in the settler.

Example 11. Phase-selective extraction of juicy grape raw materials to obtain the 1st product - grape extract insisted on the original raw material.

According to this example, the process is carried out in the installation of figure 4 with a total volume of basic equipment of 5 m ³ . In the crusher-separator 1, grapes and the whole grape pulp obtained are continuously fed and crushed with a flow rate of 1.75 m ³ / h, a sugar concentration of 180 kg / m ³ , a particle size of 0.05-5.0 mm and a porosity of 0.8 are fed into tincture 28. In tincture 28 through a recirculation line 24 continuously with a flow rate of 1 m ³ / h serves part of the extract obtained in the extractor 3 with a sugar content of 144 kg / m ³ . The mixture is kept in tincture 28 at a temperature of up to 60 ° C with stirring for up to 1 hour.

Then, the pulp insisted on the feedstock in the amount of 2.75 m ³ / h is sent to the thickener-decanter of the wall pulp 25, which is used as an inclined screw auger. From the stacker 25, a product extract infused on the feedstock with a flow rate of 1.75 m ³ / h and a sugar concentration of 171 kg / m ^{3 is} taken and removed via line 26.

Dripped-off the pulp at a rate of 1 m ³ / h, the sugar concentration of 160 kg / ^m3 and a porosity of 0.65 is sent via line 27 to mixer 2. The mixer 2 by the recirculation line 23 is also at a rate of 1 m ³ / h is fed to another part of the resulting extractor 3 extracts with a sugar content of 171 kg / m ³ . The mixture of the top pulp and extract in the mixer 2 is kept at a temperature of up to 60 ° C with stirring for up to 1 hour.

The grape pulp obtained in mixer 2 with a porosity of 0.83 is supplied by pump 6 with a flow rate of 2 m ³ / h to the inner tube 8 of the extractor 3. An extractor with a screw device in the inner tube of FIG. 3 is used. A countercurrent pump 9 feeds fresh extractant into the casing 10 of the extractor — water with a flow rate of 0.58 m ³ / h plus a liquid phase with a flow rate of 1.42 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant 0.33. Total consumption of extractant supplied to the casing of the extractor, 2 m ³ / h

The operation of the extractor 3 is carried out, as in example 1. From the casing 10 of the extractor 3 extract extract of the pulp, part of which with a flow rate of 1 m ³ / h and a sugar content of 144 kg / m ^{3 is} sent, as noted above, through line 24 to tincture 28 The extracted pulp with a flow rate of 2 m ³ / h and a porosity of 0.83 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a screw press, where it is divided into phases. From the thickener-decanter 5, the extracted grape squeeze is withdrawn with a flow rate of 0.58 m ³ / h, a sugar content of 27.4 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 1.42 m ³ / h via line 20 is returned, as noted above, to mix with the pump 9 fed into the extractor 3 with fresh extractant 0.58 m ³ / h. The degree of phase-selective extraction of sugar from raw materials is 0.95. The specific volumetric productivity of extracted sugar is 59.9 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 39.4 kg / (h · m ³ ).

Example 12. Phase-selective extraction of low-fat raw materials of sugar beet root crops with water to obtain the 1st product - infused beetroot extract.

According to this example, the process is carried out in the installation of figure 4 with a total volume of basic equipment of 5 m ³ . Beetroot and beet grinder 1 are continuously fed and ground beets and the resulting whole beet pulp with a flow rate of 1.75 m ³ / h, a sugar concentration of 180 kg / m ³ , a particle size of 0.05-5 mm and a porosity of 0.8 are fed into the tincture 28 A portion of the extract obtained in the extractor 3 with a sugar content of 107 kg / m ^{3 is} fed continuously to the tincture 28 via a recirculation line 24 continuously with a flow rate of 1.35 m ³ / h. The mixture is kept in tincture 28 at a temperature of up to 80 ° C with stirring for up to 1 hour.

Next, the pulp insisted on the feedstock in the amount of 3.1 m ³ / h is sent to the thickener-decanter pulp 25, which is used as an inclined auger stacker. Beetroot extract infused on the feedstock with a flow rate of 2.1 m ³ / h and a sugar concentration of 142 kg / m ^{3 is} selected from stacker 25.

A glass pulp with a flow rate of 1 m ³ / h, a sugar concentration of 160 kg / m ³ and a porosity of 0.65 is sent to the mixer 2. Into the mixer 2 through a recirculation line 23 with a flow rate of 0.16 m ³ / h serves part of the extract obtained in the extractor 3 with a sugar content of 107 kg / m ³ . A mixture of beet pulp and extract in a mixer 2 is kept at a temperature of up to 80 ° C with stirring for up to 1 hour.

The beet pulp obtained in mixer 2, with a porosity of 0.7, is pumped 6 with a flow rate of 1.16 m ³ / h into the inner tube 8 of the extractor 3. A countercurrent pump 9 is fed to the extractor casing 10 with fresh extractant — water with a flow rate of 0.58 m ³ / h plus the liquid phase with a flow rate of 0.58 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant 0.33. Total consumption of extractant supplied to the casing of the extractor, 1.16 m ³ / h

The operation of the extractor 3 is carried out, as in example 1. From the casing 10 of the extractor 3 is removed the extract of beet pulp, part of which with a flow rate of 1.35 m ³ / h and a sugar content of 107 kg / m ^{3 is} sent, as noted above, to tincture 28 The extracted pulp with a flow rate of 1.16 m ³ / h and a porosity of 0.7 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a screw press, where it is divided into phases. Extracted pulp is removed from the thickener-decanter 5 with a flow rate of 0.58 m ³ / h, a sugar content of 27.4 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 0.58 m ³ / h through line 20 is returned, as noted above, to mix with the pump 9 fed into the extractor 3 with fresh extractant 0.58 m ³ / h. The degree of phase-selective extraction of the component from the feed is 0.95. The specific volumetric productivity of extracted sugar is 59.9 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 39.4 kg / (h · m ³ ).

Example 13. Phase-selective extraction of juicy raw grapes with the receipt of 2 products: infused natural juice and extract of the highest pulp.

In this example, the process is carried out in the installation of figure 5 with a total volume of basic equipment of 5 m ³ . The grapes and the whole grape pulp obtained are continuously fed and crushed into the crusher-comb separator 1 with a flow rate of 1.75 m ³ / h, a sugar concentration of 180 kg / m ³ , a particle size of 0.05-5 mm and a porosity of 0.8 are fed to the tincture 28 The pulp is kept in tincture 28 at a temperature of up to 60 ° C with stirring for up to 1 hour.

Next, the infused pulp in the amount of 1.75 m ³ / h is sent to the thickener-decanter of the infused pulp 25, which is used as an inclined screw auger. From the stacker 25, the first product is selected - infused natural grape juice with a flow rate of 0.75 m ³ / h and a sugar concentration of 207 kg / m ³ and a high reduced extract.

A glass pulp with a flow rate of 1 m ³ / h, a sugar concentration of 160 kg / m ³ and a porosity of 0.65 is sent to mixer 2. Into mixer 2, a part of the extract obtained in extractor 3 is also fed with a flow rate of 1 m ³ / h with sugar content 144 kg / m ³ . The mixture of the top pulp and extract in the mixer 2 is kept at a temperature of up to 60 ° C with stirring for up to 1 hour.

The grape pulp obtained in mixer 2 with a porosity of 0.83 is supplied by pump 6 with a flow rate of 2 m ³ / h to the inner tube 8 of the extractor 3. An extractor with a screw device in the inner tube is used. A countercurrent pump 9 feeds fresh extractant into the casing 10 of the extractor — water with a flow rate of 0.58 m ³ / h plus a liquid phase with a flow rate of 1.42 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant 0.33. Total consumption of extractant supplied to the casing of the extractor, 2 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

From the casing 10 of the extractor 3, the extract of the pulp is removed, part of which is fed to mixer 2 with a flow rate of 1 m ³ / h, and the other part with a flow rate of 1 m ³ / h and with a sugar content of 144 kg / m ^{3 is} taken as the 2nd product of the process . The extracted pulp with a flow rate of 2 m ³ / h and a porosity of 0.83 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a screw press, where it is divided into phases. From the thickener-decanter 5, the extracted grape squeeze is withdrawn with a flow rate of 0.58 m ³ / h, a sugar content of 27.4 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 1.42 m ³ / h via line 20 is returned, as noted above, to mix with the pump 9 fed into the extractor 3 with a fresh extractant of 0.58 m / h. The degree of phase-selective extraction of sugar from raw materials is 0.95. The specific volumetric productivity of extracted sugar is 59.9 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 37.4 kg / (h · m ³ ).

Example 14. Phase-selective extraction of juicy raw currant berries with the receipt of 2 products: infused natural juice and extract of the highest pulp.

In this example, the process is carried out in the installation of figure 5 with a total volume of basic equipment of 5 m ³ . Currant berries and whole currant pulp with a flow rate of 1.75 m ³ / h, a sugar concentration of 180 kg / m ³ , a particle size of 0.05-4 mm and a porosity of 0.8 are fed into the roll crusher-separator 1 continuously and crushed. tincture 28. The pulp is kept in tincture 28 at temperatures up to 50 ° C with stirring for up to 1 hour.

Next, the infused pulp in the amount of 1.75 m ³ / h is sent to the thickener-decanter of the infused pulp 25, which is used as an inclined screw auger. From the stacker 25, the first product is selected — infused natural currant juice with a flow rate of 0.75 m ³ / h and a sugar concentration of 207 kg / m ³ .

A glass pulp with a flow rate of 1 m ³ / h, a sugar concentration of 160 kg / m ³ and a porosity of 0.65 is sent to mixer 2. Into mixer 2, a part of the extract obtained in extractor 3 is fed with a flow rate of 1 m ³ / h with a content of 3 sugar 141 kg / m ³ . The mixture of the top pulp and extract in the mixer 2 is maintained at a temperature of up to 40 ° C with stirring for up to 1 hour.

Obtained in the mixer 2 currant pulp with a porosity of 0.83 serves pump 6 with a flow rate of 2 m ³ / h in the inner tube 8 of the extractor 3. Use the extractor with a screw device in the inner tube. Countercurrent to the pulp, pump 9 into the casing 10 of the extractor serves fresh extractant - water with a flow rate of 0.7 m ³ / h plus a liquid phase with a flow rate of 1.3 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant is 0.4. Total consumption of extractant supplied to the casing of the extractor, 2 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

Because the casing 10 of the extractor 3 is withdrawn extract was dripped-off of pulp, of which a rate of 1 m ³ / h is fed to the mixer 2, and another part of a flow rate of 1 m ³ / h and a sugar content 141 kg / m ³ is withdrawn as a 2nd process product . The extracted pulp with a flow rate of 2 m ³ / h and a porosity of 0.83 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a reverse filter, where it is separated into phases. From the thickener-decanter 5, the extracted currant squeeze is withdrawn with a flow rate of 0.7 m ³ / h, a sugar content of 27.4 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 1.3 m ³ / h through line 22 is returned, as noted above, to mix with the pump 9 fed into the extractor 3 with a fresh extractant of 0.7 m ³ / h. The degree of phase-selective extraction of sugar from raw materials is 0.94. The specific volumetric capacity for extracted sugar is 59.3 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 37.0 kg / (h · m ³ ).

Example 15. Phase-selective extraction of juicy raw grapes with the receipt of 2 products: natural juice - gravity wort and extract of the highest pulp.

In this example, the process is carried out in the installation of Fig.6. Moreover, the total volume of the used basic equipment is 4 m ³ . In the crusher-separator 1, grapes and whole grape pulp obtained are continuously fed and crushed with a flow rate of 1.75 m ³ / h, a sugar concentration of 180 kg / m ³ , a particle size of 0.05-5 mm and a porosity of 0.8 are sent to the thickener pulp decanter 25, which is used as an inclined auger stacker. From the stacker 25, the first product is selected - natural grape juice with a flow rate of 0.75 m ³ / h and a sugar concentration of 207 kg / m ³ .

A glass pulp with a flow rate of 1 m ³ / h, a sugar concentration of 160 kg / m ³ and a porosity of 0.65 is sent to mixer 2. Into mixer 2, a part of the extract obtained in extractor 3 is also fed with a flow rate of 1 m ³ / h with sugar content 144 kg / m ³ . The mixture of the top pulp and extract in the mixer 2 is kept at a temperature of up to 60 ° C with stirring for up to 1 hour.

The grape pulp obtained in mixer 2 with a porosity of 0.83 is supplied by pump 6 with a flow rate of 2 m ³ / h to the inner tube 8 of the extractor 3. An extractor with a screw device in the inner tube is used. A countercurrent pump 9 feeds fresh extractant into the casing 10 of the extractor — water with a flow rate of 0.58 m ³ / h plus a liquid phase with a flow rate of 1.42 m ³ / h from thickening in the thickener-decanter 5 of the extracted pulp. The relative dose of fresh extractant 0.33. Total consumption of extractant supplied to the casing of the extractor, 2 m ³ / h

The operation of the extractor 3 is carried out, as in example 1.

From the casing 10 of the extractor 3, the extract of the pulp is removed, part of which is fed to mixer 2 with a flow rate of 1 m ³ / h, and the other part with a flow rate of 1 m ³ / h and with a sugar content of 144 kg / m ^{3 is} taken as the 2nd product of the process . The extracted pulp with a flow rate of 2 m ³ / h and a porosity of 0.83 is removed from the extractor 3 through line 7 to a thickener-decanter 5, which is used as a screw press, where it is divided into phases. From the thickener-decanter 5, the extracted grape squeeze is withdrawn with a flow rate of 0.58 m ³ / h, a sugar content of 27.4 kg / m ³ and a porosity of 0.4. And the liquid phase with a flow rate of 1.42 m ³ / h via line 22 is returned, as noted above, to mix with the pump 9 fed into the extractor 3 with fresh extractant 0.58 m ³ / h. The degree of phase-selective extraction of sugar from raw materials is 0.95. The specific volumetric productivity of extracted sugar is 74.9 kg / (h · m ³ ). For the well-known 3-stage installation of mixing-separation of phases, these values are equal: 0.75 and 37.4 kg / (h · m ³ ).

The main comparative parameters and the results of the above examples of phase-selective extraction in a solid-liquid system are presented in the table.

An analysis of the data presented in the table determines the optimal values of the parameters of phase-selective extraction processes. According to this invention, for extracted types of solid-phase, low-fat and juicy raw materials, such parameters are: the size of the dispersed particles of the extracted pulp of the raw material in the range of 0.05-5.0 mm, the porosity of the pulp supplied to the extractor in the range of 0.6-0.83, the relative dose used fresh extractant to the volume of processed raw materials in the range of 0.33-1.0. Moreover, for phase-selective extraction according to the present invention, in comparison with a 3-stage mixing-phase separation process, the degree of component extraction from raw materials is 1.2-1.3 times greater, the specific volumetric productivity of the equipment for the extracted component is 1.5-2.5 times greater. And this is with the smaller according to this invention in 2.4-4 times the number of technological operations and units of equipment used.

The proposed installation phase-selective extraction according to this invention solves the technical problem of the invention for the device. The capabilities of the installation for carrying out various options of extraction processes on it, processing various types of solid-phase, low-fat and juicy raw materials with obtaining several types of products: extracts, extracts infused with raw materials extracts, natural juices and infused natural juices have been increased. The capabilities of the control modes are increased, the mass transfer rates, the specific productivity, the compactness of the equipment and the stability of its operation are increased.

The proposed method of phase-selective extraction according to this invention solves the technical problem of the invention by the method. The optimal options and modes of the processes of extraction, processing of various types of solid-phase, low-fat and succulent raw materials are increased and several types of products are obtained: extracts, extracts infused with the raw materials, natural juices. An increase in the degree of extraction of components from raw materials, the specific volumetric productivity of equipment for the extracted component in comparison with known methods is shown in a number of examples.

Table
Comparative parameters of phase-selective extraction processes in a solid-liquid system No. at measure Raw materials - extractant - component: process parameters The extraction process in a 3-stage mixing-separation unit Phase Selective Extraction Process one 2 3 four one Flax seeds - water - solids: - relative dose of fresh extractant 1,0 1,0 - degree of extraction 0.75 0.9 - specific productivity of equipment, kg / (h · m ³ ) 12.5 thirty 2 Soya beans - water - solids: - relative dose of fresh extractant 1,0 1,0 - degree of extraction 0.75 0.9 - specific productivity of equipment, kg / (h · m ³ ) fifteen 36 3 Nougat Beans - Water - Solids: - relative dose of fresh extractant 1,0 1,0 - degree of extraction 0.75 0.9 - specific productivity of equipment, kg / (h · m ³ ) 13.8 33 four Lentils - water - solids: - relative dose of fresh extractant one 0.67 - degree of extraction 0.75 0.9 - specific productivity of equipment, kg / (h · m ³ ) 14,4 34.5 5 Oilseed grains - gasoline - oil: - relative dose of fresh extractant 1,0 1,0 - degree of extraction 0.75 0.94 - specific productivity of equipment, kg / (h · m ³ ) 40 one hundred 6 Grain mash - water - solids: - relative dose of fresh extractant one 0.83 - degree of extraction 0.75 0.89 - specific productivity of equipment, kg / (h · m ³ ) twenty 47.5 7 Malt mash - water - solids: - relative dose of fresh extractant one 0.69 - degree of extraction 0.75 0.91 - specific productivity of equipment, kg / (h · m ³ ) 18.8 45.5 8 Sugar beet - water - sugar: - relates. dose of fresh extractant one 0.83 - degree of extraction 0.75 0.93 - specific productivity of equipment, kg / (h · m ³ ) 22.5 56 9 Apples - Water - Sugar: - relative dose of fresh extractant one 0.91 - degree of extraction 0.75 0.89 - specific productivity of equipment, kg / (h · m ³ ) 17.5 41.5 10 Precipitation - water - solids: - relative dose of fresh extractant one 0.83 - degree of extraction 0.75 0.91 - specific productivity of equipment, kg / (h · m ³ ) 16.3 39.3 eleven Grapes - water - sugar: - relative dose of fresh extractant one 0.33 - degree of extraction 0.75 0.95 - specific productivity of equipment, kg / (h · m ³ ) 39,4 59.9 12 Sugar beet - water - sugar: - relative dose of fresh extractant one 0.33 - degree of extraction 0.75 0.95 - specific productivity of equipment, kg / (h · m ³ ) 39,4 59.6 13 Grapes - water - sugar: - relative dose of fresh extractant one 0.33 - degree of extraction 0.75 0.95 - specific productivity of equipment, kg / (h · m ³ ) 37,4 59.9 fourteen Currants - water - sugar: - relative dose of fresh extractant one 0.4 - degree of extraction 0.75 0.94 - specific productivity of equipment, kg / (h · m ³ ) 37 59.3 fifteen Grapes - water - sugar: - relative dose of fresh extractant. one 0.33 - degree of extraction 0.75 0.95 - specific productivity of equipment, kg / (h · m ³ ) 37,4 74.9

Information sources

1. Kasatkin A.G. Basic processes and apparatuses of chemical technology. M., Chemistry, 1971, p. 584.

2. Romankov P.G., Kurochkina M.I. Extraction from solid materials. Leningrad, Chemistry, 1983, p.138.

3. SU 548290 A1, 02.28.1977, BI No. 8.

4. SU 1220180 A1, 04/10/96, BI No. 10.

Claims (17)

1. Installation for phase-selective extraction in a solid-liquid system, containing a crusher connected in series, a mixer with a liquid supply pipe, a shell-and-tube extractor pipe in a pipe with a convectively permeable inner pipe, an extractor pulp thickener-decanter with a liquid phase discharge pipe from it, pumps for counterflow pulp supply from the mixer to the pipe and extractant to the casing, recirculation and technological pipelines, characterized in that the mixer is connected by pipelines the house with the extract exit from the extractor housing, the pipeline for removing the liquid phase from the thickener-decanter of the extracted pulp is connected to the extractant inlet to the extractor, the extractor housing is divided by longitudinal partitions into an even number of channels with extractant inlets, nozzles and an extract pump for extracting them, installation it is also equipped with a pulsation system, including valves on these nozzles and a control computer, ensuring their cross opening and closing. 2. Installation according to claim 1, characterized in that it is equipped with a thickener-decanter pulp installed between the crusher and the mixer. 3. Installation according to claim 1, characterized in that it is equipped with a tincture installed between the crusher and the thickener-decanter pulp. 4. Installation according to claim 3, characterized in that the tincture is made in the form of a vertical or horizontal cylindrical sectioned apparatus with mixers in sections and a thermostatic jacket on the body. 5. Installation according to claim 3, characterized in that the tincture is connected by a pipe to the outlet of the extract from the casing of the extractor. 6. The apparatus according to claim 1, characterized in that a hammer mill, or a roller mill, or a disk mill, or a millstone, or a grain mill, or a beet slicer mill, or a crusher separator, or a malt grinder are used as the crusher. 7. Installation according to claim 1, characterized in that as a thickener-decanter use a hydrocyclone, or a reversible filter, or a centrifugal separator, or a stacker, or a screw press, or a sump. 8. Installation according to claim 1, characterized in that the convectively permeable inner tube of the extractor is made of perforated or porous metal, plastic, ceramic, cermet or reinforced composite material. 9. Installation according to any one of paragraphs.1 and 8, characterized in that the convective-permeable inner tube of the extractor is made with holes in the range of 0.03-1.0 mm 10. Installation according to claim 1, characterized in that a screw device with a rotation drive is installed in the inner tube of the extractor. 11. A method of phase-selective extraction in a solid-liquid system, including crushing the raw material, mixing it with a liquid to produce a flowing pulp, counter-current convective mass transfer between pulp and extractant flows in adjacent channels with permeable walls when alternating pressure drops are created between them for multiple transverse exchange streams in portions of the liquid phase to obtain extracted pulp and extract, thickening the extracted pulp and returning the resulting liquid phase in percent ss, characterized in that the crushed raw material is mixed with the recirculated extract, and obtained by condensation of the extracted pulp is mixed with the liquid phase supplied to the extraction of fresh extractant. 12. The method according to claim 11, characterized in that the crushed juicy raw material is concentrated with the selection of the first product - natural juice, and the top pulp is mixed with part of the extract and sent for extraction to obtain a second product - extract. 13. The method according to claim 11, characterized in that the crushed low-fat raw materials are mixed with a portion of the extract, infused and concentrated to obtain a product infused extract, and the condensed pulp is mixed with the rest of the extract and sent for extraction. 14. The method according to claim 11, characterized in that the crushed juicy raw materials are infused and concentrated with the selection of the first product - infused natural juice, and the top pulp is mixed with a portion of the extract and sent for extraction to obtain a second extract product. 15. The method according to any one of claims 11-14, characterized in that the raw materials are crushed to the size of dispersed particles in the range of 0.05-5.0 mm. 16. The method according to any one of claims 11-14, characterized in that the porosity in the range of 0.6-0.83 is maintained in the raw material supplied to the extractor. 17. The method according to any one of paragraphs.11-14, characterized in that the relative dose of fresh extractant used to the volume of processed raw materials is maintained within the range of 0.33-1.0.

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