Heat-and-mass exchanger

FIELD: mechanics.

SUBSTANCE: proposed heat-and-mass exchanger is intended for interaction of gas and fluid and can be used for cooling and purification of the contact gas from catalyst dust and steam stripping of hydrocarbons from water condensate in production of styrene by ethyl benzene dehydrogenation. The cylindrical casing top accommodates fluid intake and gas discharge branch pipes while the cylindrical casing bottom has fluid discharge branch pipe and the gas main feed pipeline. Just above the latter, a baffle followed by one or several disks and a device for gas and fluid to interact therein. The said disk feature central bores. Note here that the lower disk bore diameter is smaller than that of the gas feed pipeline, and that the bore diameters of the upper disk are smaller than those of the lower disks. The disks in question have the diameter equal to that the baffle.

EFFECT: higher efficiency of mass-and-heat transfer due to improved gas flow distribution over exchanger diameter.

12 cl, 2 dwg, 1 tbl

 

The invention can find application in the oil refining, petrochemical, chemical and other industries. It may be effective to use the invention, in particular, in the field of production vinylaromatic hydrocarbons, such as styrene, alphamethyl-styrene, vinyltoluene, divinylbenzene, as well as isoprene, butadiene and other

Known scrubber with a regular nozzle for effecting heat exchange processes, including dust control, when a counter-current movement of the gas and the liquid layer on the nozzle (Vnwa, Ajovalasit. Preparation of industrial gases to be purged. Moscow, Publishing house "Chemistry", 1975, p.85). The scrubber has a fitting for gas inlet located in the side wall of the shell of the apparatus under the packing layer. The disadvantage of this apparatus is the low efficiency of heat exchange processes, high hydraulic resistance and the formation of dust deposits on the surface of the nozzle.

Also known foam machine - gazopromyvateli for air purification from dust in apatitonefelinovoj processing industry, comprising a vertical rectangular enclosure containing a node entry of air into the apparatus in the form of a side fitting (cone) and located above the device for shielding in the form of one of the perforated grille (Mesin, Ispahan is in, Alacart. Foam scrubbers, heat exchangers and absorbers, Goskomizdat, 1959, p.47).

Known apparatus has a low strength box-shaped housing with flat walls and an uneven distribution of gas flow cross-sectional area contacting with the side entry of gas into the apparatus and low efficiency of heat transfer.

The closest in technical essence to the present invention is heat-mass exchange apparatus for interaction between the gas and the liquid used for capture of hydrogen fluoride from gases from electrolytic aluminum production. Known foam apparatus includes a vertical cylindrical casing containing in its upper part the nozzles for liquid inlet and outlet for the gas outlet, and the bottom pipe for withdrawal of fluid and the Central pipeline for gas from above the upper edge series along the gas stream, the gas distribution grid and apparatus for contacting gas and liquid in the form of two perforated annular gratings (Ispahani, Alamarat. Penn mode and foam machines. Publishing House "Chemistry". 1977, str). The device contains also located in the Central part of the grating distribution box of cylindrical form, from which the release irrigating soda is th solution is in the interval between the gas distribution grid and the lower perforated grille. At the entrance to the inlet to the gas outlet installed britholite with the drain pipe, the lower end of which is located in the volume of the selection box to enter irrigating soda solution.

This unit has a more rugged housing that is provided with the cylindrical shape of the shell, a better distribution of gas flow through the Central pipe with a baffle and advantage in the efficiency of heat transfer in comparison with the above foam machine.

At the same time, the apparatus has the following disadvantages.

Gas distribution grid established on all of the cross-section of the apparatus, does not provide the necessary uniform distribution of gas flow in the zone of contact (area of installation annular perforated gratings) in respect of:

- feed gas stream in the parietal area of the gas distribution grid;

with uneven flow distribution grid irrigating fluid (in the Central part thereof);

- distorted currents distributed over the whole cross section of the apparatus of the gas stream bottom part of the distribution boxes in front of the entrance flow in the annular area of contact.

Significant uneven distribution of gas flow in the zone of contact determines insufficient talamasca the s in the device.

In addition, the apparatus has a high hydraulic resistance associated with the use of irrigated distributive lattice and a combination of two perforated gratings in the ratio of their free sections in region 1÷1,35.

In view of these disadvantages of the known foam device in large processes, such as the method of producing styrene by dehydrogenation of ethylbenzene (with the diameter of the device up to six meters or more), encounters considerable difficulties.

The present invention is to increase the efficiency of the heat transfer in the apparatus while improving the distribution uniformity of the gas flow in the zone of contact and the reduction of hydraulic resistance.

Features of heat and mass transfer apparatus for interaction between gas and liquid, comprising a vertical cylindrical housing with connections for liquid inlet and outlet for the gas outlet in its upper part, a pipe for withdrawal of fluid and the Central pipe to enter the gas stream and apparatus for contacting gas and liquid over it - in its lower part. Between the top of the pipeline for gas inlet and a baffle installed one or more disks having a diameter equal to the diameter of the bump, with the Central hole of each, if e is ω diameter of the hole at the bottom of the disc is less than the diameter of the pipeline to the gas inlet, while the upstream disk hole diameter smaller than the downstream.

Specified bumpers may be made in the form of a flat disk or in the form of a cone with the apex directed upwards, and may also be perforated.

The disk or disks in the apparatus is preferably located at the same distance from the top edge of the pipeline to enter the gas from each other and from the bumper, when this specified distance is:

where H is the distance from the top edge of the pipeline for input gas to the lower disk, the distance between the disks, the distance from the top drive to the bumper, m;

FTr- the cross-sectional area of the pipeline to enter the gas, m2;

- the sum of the diameters of the holes of the discs and the diameter of the pipeline to enter the gas, m;

n=1÷5 - number of discs;

K=0.5÷1.0 - factor.

Device for interaction between gas and liquid can be made in the form of two perforated annular grids between which the Central part is a switch box of cylindrical shape. At the entrance to the inlet to the gas outlet installed britholite with the drain pipe. Preferably, the free section of the lower grille was 1.4÷3.5 times more free top section is th lattice, and the ratio of the diameters of the bump and junction boxes were in the range of 1:0.5 to÷1,5.

The distance between the gratings may be 0.1÷0.4 diameter of the body of the device.

The bottom end of the drain pipe britholite preferably be positioned in the volume of distribution boxes.

The distribution box may be provided with a drain pipe, the lower end of which is located below the top edge of the pipeline for gas injection.

As a device to communicate the gas and the liquid can also be installed, for example, a layer of regular mass transfer nozzle, package of lattices, the package of plates, or a combination of grids and nozzles. While on the device include a liquid distributor which is connected with the pipes to enter the liquid.

The distance between the bump stop and the device for interaction between the gas and the liquid may preferably be 1÷0.4 diameter of the body of the device.

The proposed heat and mass transfer apparatus for interaction between gas and liquid can be used in different processes, petrochemical, chemical industry, for example in the production of styrene by dehydrogenation of ethylbenzene.

Figure 1 shows a diagram of one embodiment of the inventive apparatus - foam device for cooling and cleaning the contact gas from the catalyst dust and the parks of hydrocarbons from water condensate in the process of producing styrene by dehydrogenation of ethylbenzene.

The apparatus has a vertical cylindrical body 1, a Central pipe for the gas inlet 2 is located above the upper edge 3 in series along the gas asymmetrically to the casing disks with Central holes 4 and 5, the bump 6, the perforated annular gratings 7 and 8. The space between the upper edge of the Central pipeline gas inlet and a baffle divides the disk into three chambers 9, 10 and 11. The device contains also located in the Central part of the grating distribution box of cylindrical form 12 with the upper edge 13 for overflow of liquid from the top of the lattice. At the entrance to the inlet to the gas outlet 14 is installed britholite 15 with the drain pipe 16, the lower end of which 17 are located in the volume of distribution boxes. A switch box provided with a drain pipe 18, the lower end 19 which is located below the liquid level in the bottom part of the apparatus. The apparatus has a nozzle 20 for entering fluid, the annular receiving box 21 with the annular overflow threshold 22 on the upper grate fitting 23 for measuring the liquid level in the bottom part of the device, the fitting 24 to drain the fluid, a nozzle 25 for withdrawal of fluid from the apparatus and hatches 26 for cleaning and repair of the device.

Contact the gas enters the apparatus through the pipe 2, is divided into two discs 4, 5 and the bump 6 on three happy the actual directional flow. Due to the fact that the pressure in front of the disks in the cells, respectively, 9, 10 and 11 differ from each other (consistently falls), the flow rate of the gas flows of the downstream chambers is higher than the flow rate from the upstream chambers. In this regard, lower stream flows in located at a greater distance parietal area of the device, and the upper in its Central part. These flows do not intersect, are formed in the axial direction in the annular space and received uniformly in the annular space between the two perforated grids, which ultimately ensures the uniformity of the gas flow in this zone. Go through perforated gratings 7 and 8, the contact of the gas through britholite 15 and line 14 is directed at the stage of condensation and separation of styrene. Obtained at the stage of condensation of water condensate is routed to offer heat and mass transfer apparatus through the fitting 20 and the annular receiving box 21. The flow of water condensate uniformly irrigates the upper perforated grid 8 through the annular Weir lip 22 on the periphery of the lattice is a lattice in the radial direction, a cross-flow gas contact, and through the drain threshold formed by the upper edge 13 of the distribution box 12, the drain pipe 18, comes the t below the level of the layer of water condensate in the bottom part of the device, where through the nozzle 25 is directed to the purification and use in the process of dehydrogenation of ethylbenzene.

The upper perforated grille 8 is in the froth regime, i.e. when the intense turbulence in gas-liquid systems by transforming it into a moving unstable, but dynamically stable foam at the expense of the kinetic energy of the gas. In the claimed range of the ratio of the free cross section of the lower and upper grilles (1,4÷3,5) when the claimed location of the drain pipes of britholite and distribution boxes upper grille works in neprovalnoy liquid mode and lower grille 7 remains "dry" and works as a distribution for gas. This combination of modes gratings when the distance between the gratings of 0.1÷and 0.4 of the diameter of the body of the device, when the ratio of the diameters of the bump and distribution boxes 0,5÷1,5 provides a more uniform flow distribution in the contact area and high heat transfer with low pressure drop across the gratings in the present embodiment, heat and mass transfer apparatus.

To achieve a more uniform distribution of gas flow in the cross section of the apparatus of the distance from the top edge of the pipe 3 to the input of gas to the lower disk 4 between the discs 4 and 5 and from the top of the disk 5 to the bump 6 can be made equal is. Determination of the magnitude of this distance at the above ratio to calculate the distance H is subject to the requirements of the division of the gas stream flowing from the pipe to the gas inlet, into three equal flow directed into the chambers 9, 10 and 11. This requirement is accomplished by the equality of the square Central hole of the upper disk 5 and squares of the rings conventionally formed in the projection along the axis of the apparatus (along the gas flow) of the circumferences of the Central holes of the upper and lower disk, and the center hole of the lower disk and piping for gas injection. The area of the Central hole of the upper disk F1=1/3 FTrand the lower disk F2=2/3 FTrand accordingly, the diameters of the Central openings of these disks will be 0,577 and 0,816 the diameter of the pipeline for gas injection.

For example, when the pipeline diameter is 1.4 m (FTr=0,785·1,42=1.54 m2), the diameter of the Central hole of the upper disk is ˜ 0,577·1,4=0.81 m and lower disc ˜ 0,816·1,4=1,14 m the distance H (in accordance with the above value for calculation) will be: 0,72·1,54/1,4+1,14+0,81=0,33 m

Increasing the number (n) of the installed drives over 5 unnecessarily complicates the design. At the same time reducing the K-factor in Pref is given to the relation for calculation to a value of less than 0.5 leads to an unjustified increase of the hydraulic resistance of the device, and increased To above 1.0 leads to an excessive increase in the size and metal of the device.

The effectiveness of the proposed heat and mass transfer apparatus in designs using as a device to communicate the gas and the liquid layer regular mass transfer nozzle, package of lattices, pack plates or a combination of grids and nozzles also increases due to significantly improve the distribution of gas flows.

Figure 2 presents the option of using the proposed heat and mass transfer apparatus in the technological scheme of the process of obtaining styrene by dehydrogenation of ethylbenzene. The table below shows the material balance of heat and mass exchange apparatus, showing the efficiency of the device in the process. The technology involves the dehydrogenation of ethylbenzene in the presence of water vapor in the reactor system 27, the use of heat contact of the gas in the HRSG 28 generating water vapor used in the dehydrogenation process, the cooling and cleaning of the contact gas from the catalyst dust and Stripping of hydrocarbons from water condensation process in heat and mass transfer apparatus 29. The scheme also contains a condensation unit 30, from which the resulting aqueous condensate is directed to the irrigation of heat and mass transfer device 29, which contact the gas ohla is given with 180÷ 250°C to 70÷90°by evaporating part of the water condensate is purified from the catalyst dust in the hydraulic resistance of the device 300÷500 mm of water column. Simultaneously Stripping the hydrocarbons contained in the source water condensate. Oparanya hydrocarbons are returned to contact the gas and aqueous condensate containing the minimum amount of impurities (see the flow from up in up in the table)is sent to a purification unit water condensate 31 to prepare it for reuse in the process. Two-stage cleaning of the condensate in the proposed heat and mass transfer apparatus 29 and the node 31, for example, filtration methods of condensation from trapped dust and subsequent distillation of the condensate in the presence of a solvent (benzene-toluene fraction) allows to obtain the purity of the water of condensation (see the flow from up in AP and in the system of water circulation in the table), sufficient for use as a supply of waste heat boilers with obtaining the secondary vapor directed to the dilution in the dehydrogenation of ethylbenzene.

The hydrocarbon part condensed in the condensation unit 30 products sent to node isolation and purification of styrene 32.

The hydrocarbon part condensed in the condensation unit 30 products sent to site selection and the cleaning of styrene 32.

Table
The material balance of heat and mass transfer apparatus.
Component nameContact the gas, kg/hWater condensate, kg/h
InputOutputInputOutputWith purification unit water condensate
The name of the streamFrom up in APFrom up in APFrom up in APFrom up in APFrom up in AP and in the water circulation system
Hydrogen348348
Methane4646
Ethylene2222
Carbon dioxide374374
Benzene181259791
Toluene517556402Ȋ
Waxes220
Ethylbenzene11655116711710.1
Styrene1716317191290.570.1
Xylenes1515
A-methylsterol99
Heavy residue4747
Total3037930540165,274.570.2
Water vapor (water)56846,56177462427,7257500,2257500
Only87225,59231462592,9957504,7957500,2

1. Heat and mass transfer apparatus for interaction between gas and liquid, comprising a vertical cylindrical housing with connections for liquid inlet and outlet for the gas outlet in its upper part, a pipe for withdrawal of fluid and the Central pipeline for centuries is Yes gas with a baffle and a device for interaction between the gas and the liquid above it - in its lower part, characterized in that between the upper edge of the pipeline for gas inlet and a baffle installed one or more disks having a diameter equal to the diameter of the bump, with a Central hole each, and the diameter of the hole at the bottom of the disc is less than the diameter of the pipeline to the gas inlet and the upstream disk hole diameter smaller than the downstream.

2. The apparatus according to claim 1, wherein the bump is made in the form of a flat disk or in the form of a cone with the apex directed upwards.

3. The apparatus according to claim 2, characterized in that the bump perforated.

4. The apparatus according to claim 1, characterized in that the disks are set at the same distance from the top edge of the pipeline to enter the gas from each other and from the bumper, when this specified distance is:

where H is the distance from the top edge of the pipeline for input gas to the lower disk, the distance between the disks, the distance from the top drive to the bumpers;

FTr- the cross-sectional area of the pipeline to enter the gas, m2;

- the sum of the diameters of the holes of the discs and the diameter of the pipeline to enter the gas, m;

n=(1÷5) number of discs;

K=(0.5÷1.0) factor.

5. The apparatus according to claim 1, ex is different, however, the device for interaction between the gas and the liquid is made in the form of two perforated annular grids between which the Central part is a switch box of cylindrical shape, and the inlet pipe to the gas outlet installed britholite with the drain pipe, thus the free section of the lower grilles 1.4÷3.5 times more free cross section of the upper grid, and the ratio of the diameters of the bump and distribution boxes located in the range of 1:(0.5 to÷1,5).

6. The apparatus according to claim 5, characterized in that the distance between the gratings is 0.1÷0.4 diameter of the body of the device.

7. The apparatus according to claim 5, characterized in that the bottom end of the drain pipe britholite is the volume of distribution boxes.

8. The apparatus according to claim 5, characterized in that a switch box provided with a drain pipe, the lower end of which is located below the top edge of the pipeline for gas injection.

9. The apparatus according to claim 1, characterized in that the device for interaction between the gas and the liquid layer has regular mass transfer nozzle.

10. The apparatus according to claim 1, characterized in that the device for interaction between gas and liquid is installed on the grids or plates.

11. The apparatus according to claim 1, characterized in that the device for interaction between the gas and the liquid to set the Leno combination of grids and nozzles.

12. The apparatus according to claim 1. characterized in that the distance between the bump stop and the device for interaction between gas and liquid is 0.1÷0.4 diameter of the body of the device.



 

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1 dwg

FIELD: mechanical engineering; oil-processing industry; gas-processing industry; devices for separation of the gases into fractions.

SUBSTANCE: the invention is pertaining to the field of mechanical engineering, in particular, to the process engineering of separation of the natural gas into fractions, for example, at reprocessing of the oil gases by the low-temperature condensation and may be used in the oil-processing industry and the natural gas-processing industry. The most preferable is usage of the presented device in the capacity of the deethanizer or the demethanizer. The device for separation of the gas into the fractions is made in the form of the distillation column consisting of two communicating to each other sections - the upper section and the lower section. The column has two inlets, one of which is arranged in the lower section, and another - in the upper section, and two outlets. The device contains the drips-deflector and the cooler arranged in the upper part of the upper section, the tubular components made in the form of the spiral used for the sections communication to each other and arranged in the lower part of the upper section. The sections are divided by the partition with the holes used for arrangement of the ends of the tubular components and outlets are arranged in the upper and the lower parts of the upper section accordingly. The cooler is made in the form of the hollow cylinder from the external side of which there is the tubular coil used for the coolant. The drips-deflector consists of the lower and upper cylinders, at that the upper cylinder has the smaller diameter and is arranged in the lower cylinder with the clearance concerning the bottom of the lower cylinder forming the labyrinth for passage of the fraction of the gas, and the lower cylinder has the hole for the gas withdrawing pipeline. The device is supplied with the components for condensation of the liquid and is made in the form of the feed screws arranged inside the spiral of the tubular components. The invention ensures simplification of the design of the device at improvement of the quality of separation of the hydrocarbon-containing raw.

EFFECT: the invention ensures simplification of the design of the device at improvement of the quality of separation of the hydrocarbon-containing raw.

4 cl, 2 dwg

FIELD: chemical industry; gas and oil industries; other industries; production of the heat-mass-exchange devices.

SUBSTANCE: the invention is pertaining to the apparatuses used for heat-mass-exchange processes in the systems of gas or vapor-liquid, in particular, to the rectifying, absorption columns, the heterophase reactors of the column type and may be used in various industries. The heat-mass-exchange apparatus contains the body with the connecting pipes of inlet and outlet phases and the disposed in altitude contact plates, each of which is made in the form of the base with the holes, the overflow connecting pipes and the valves, and the collector with the connecting pipes for feeding and withdrawal of the heat transfer medium. The overflow connecting pipe is arranged at the wall of the body and consists of two parts, in the upper part of which on the grating there is the nozzle, and in the lower part there is the heat exchanger made in the form of the jacket with the connecting pipes connected to the connecting pipes of the collector. Above the overflow connecting pipe there is the non-centrally mounted valve with the positive floatability. The technical result of the invention is the increased stability of the heat-mass exchange process in the gas-(vapor)-liquid streams in the broad range of variations of the consumption of the gas (vapor) and the liquid on each plate that improves the quality separations, and simplifies the design.

EFFECT: the invention ensures the increased stability of the heat-mass exchange process in the gas-(vapor)-liquid streams on each plate, improves the quality separations, and simplification the design of the heat-mass-exchange apparatus.

1 dwg

FIELD: liquid distributors for mass-exchange columns.

SUBSTANCE: proposed liquid distributor is used for distribution of liquid in lower mass-exchange layer consisting of several disordered, grid-type or structurized elements of packing. Liquid distributor is provided with many extended chutes separated from one another and laid across the column. Side walls of chutes have many liquid drain holes located in one or several planes at definite distance from chute bottom. Reflecting shields are located on the outside of chute side walls; they receive liquid through upper parts. Lower parts of reflecting shields form narrowed outlet hole located in plane below chute and used for draining liquid from reflecting shields to lower mass-exchange layer. Liquid drain holes in one of side walls of chute are displaced relative to the like holes in other side wall of chute for smooth distribution of liquid in outlet hole. Position of reflecting shields may be regulated vertically; they shall be supported by upper surface of mass-exchange layer so that liquid should be fed directly to mass-exchange layer, thus decreasing probability of entrapping falling liquid by vapor flow ascending through mass-exchange layer. Liquid escaping from outlet hole forms flow in form of curtain excluding penetration of vapor into outlet hole. Vapor admitted to outlet zone may be discharged upward through opening between shields and respective chutes at reduced velocity, thus excluding entrapping of liquid. Said opening is used for entrapping any liquid escaping from chutes by draining it downward over inner surface of reflecting shields.

EFFECT: enhanced efficiency.

33 cl, 7 dwg

FIELD: gas-production industry; oil-producing industry; other industries; methods and devices for separation of a liquid from a gas.

SUBSTANCE: the invention is pertaining to the methods for separation of a liquid from a gas and to the design solution of the devices for distribution of the gaseous and the liquid flows along the cross-section of the apparatus and separation of the liquid from the gas flow, which may be used for the processes of separation, absorption, rectification in the gas-production industry, oil-producing industry and in the apparatuses for realization of the similar production processes. The method of separation of a liquid from a gas includes: the radial feeding of the mixture into the body of the apparatus, its distribution along the cylindrical wall with the subsequent division into the radial flows directed to the axis of the apparatus and passing into the axial flows. The radial flows are divided into jets, separate them from the liquid on the surfaces located along the wall, then additionally distribute in the cross section of the apparatus. Separation of the radial flows from the liquid conduct on the vertical porous components, using which the liquid is diverted into the still bottom unit of the apparatus below the mixture feeding. The device for realization of the method of separation of the liquid from the gas includes the perforated shell established inside the body of the apparatus opposite to the gas inlet fitting pipes with a clearance to the body overlapped by partition in its upper part. On the shell opposite to the perforation there are the vertically orientated rows of the porous volumetric components overlapping the channels of the perforation. The clearance between the shell and the body and the top of the shell are overlapped by the semi-dead plate with the gas passage fitting pipes connected with the internal cavity of the shell. The shell in its lower part has the water lock or is partially overlapped. It is made out of out the plane components closed by the body of the apparatus. The invention allows to increase efficiency of the separation and to reduce ablation of the liquid.

EFFECT: the invention ensures the increased efficiency of the separation and reduction of the liquid ablation.

5 cl, 2 dwg

FIELD: cryogenic engineering, in particular, devices for separation of crypton-xenon concentrate obtained at air-separating installations.

SUBSTANCE: the mass-transfer apparatus has a contact device including the concentration and exhausting sections filled with packings, inlet chamber, condenser-evaporator, still with an electric heater and evaporator, still with an electric heater and evaporator. In addition, the inlet chamber of the feed flow of the mass-transfer apparatus (rectifying column) has a packing section with a specific surface less than the specific surface of the packing of the concentration section, is provided with a heater and a thermal converter, and the feed flow branch pipe- with a thermal bridge. The concentration and exhausting sections have different dimensions of the free cross-sectional areas, have reflux distributors and redistributors spaced in height at distance L=(150 to 300)d equiv; where d equiv. - the equivalent diameter of the packing, perforated tubular vertical inserts are additionally installed in the drain holes of the bottoms of the reflux distributors and redistributors. The straight-tubular tube still of the condenser of the intermediate heat-transfer agent has at least one duct, whose cross-sectional area is commensurable with the total area of the flow areas of the heat-transfer tubes, and the still electric heater - the heat-transfer base with an electric heating element packed and covered with heat-transfer powder and pressed to the still bottom by pull rods provided with springs.

EFFECT: enhanced reliability of the mass-transfer apparatus and reduced specific amount of metal per structure.

6 dwg

FIELD: cryogenic engineering, in particular, devices for separation of crypton-xenon concentrate obtained at air-separating installations.

SUBSTANCE: the mass-transfer apparatus has a contact device including the concentration and exhausting sections filled with packings, inlet chamber, condenser-evaporator, still with an electric heater and evaporator, still with an electric heater and evaporator. In addition, the inlet chamber of the feed flow of the mass-transfer apparatus (rectifying column) has a packing section with a specific surface less than the specific surface of the packing of the concentration section, is provided with a heater and a thermal converter, and the feed flow branch pipe- with a thermal bridge. The concentration and exhausting sections have different dimensions of the free cross-sectional areas, have reflux distributors and redistributors spaced in height at distance L=(150 to 300)d equiv; where d equiv. - the equivalent diameter of the packing, perforated tubular vertical inserts are additionally installed in the drain holes of the bottoms of the reflux distributors and redistributors. The straight-tubular tube still of the condenser of the intermediate heat-transfer agent has at least one duct, whose cross-sectional area is commensurable with the total area of the flow areas of the heat-transfer tubes, and the still electric heater - the heat-transfer base with an electric heating element packed and covered with heat-transfer powder and pressed to the still bottom by pull rods provided with springs.

EFFECT: enhanced reliability of the mass-transfer apparatus and reduced specific amount of metal per structure.

6 dwg

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