Device for separating a gas-liquid mixture containing ammonium carbamate

Abstract

The utility model relates to devices for separating a gas-liquid mixture containing ammonium carbamate in urea production plants. What is proposed is a device for separating a gas-liquid mixture containing ammonium carbamate, comprising: a housing having an upper part and a lower part, an inlet pipe for supplying a gas-liquid mixture, an outlet pipe for removing separated liquid, and an outlet pipe for removing gas. Disposed in the lower part are mass transfer trays, wherein the inlet pipe for supplying a gas-liquid mixture is disposed in the lower part below the mass transfer trays, and the outlet pipe for removing separated liquid is disposed in the lower part above the mass transfer trays. The mass transfer trays are arranged at a distance H5 from one another, which is equivalent to 0.4-1.5 of the diameter D3 of the lower part. The technical result is an increase in the operating efficiency of the device, which is manifest in a high ammonium carbamate content in the solution removed from the device and the ability to provide the desired temperature of the liquid phase at the outlet from the device, in addition to a reduction in the metal requirement of the device.

Description

[0001] DEVICE FOR SEPARATION OF GAS-LIQUID MIXTURE CONTAINING AMMONIUM CARBAMATE

[0002] Field of technology

[0003] This utility model relates to devices for separating gas-liquid mixtures containing ammonium carbamate in urea production units. It enables the separation of the gas and liquid phases after the carbamate condenser in a high-pressure unit, reactions to form carbamate and urea, and subsequent feeding of the separated liquid phase to a urea production reactor. The device can be used in the chemical and fertilizer industries.

[0004] State of the art

[0005] A condenser containing a scrubber at the top is disclosed in U.S. Patent Applications US20060270872A1, published November 30, 2006, and US20090036712A1, published February 5, 2009. Recycled carbamate liquid is fed into the scrubber as an absorbent medium. In the scrubber, the recycled carbamate liquid undergoes gas-liquid separation within the condenser, contacts gaseous components rising from the gas-liquid interface, absorbs portions of the ammonia and carbon dioxide contained in these gaseous components, passes through a downcomer, and is fed to the bottom of the condenser.

[0006] A U-tube is installed inside the condenser as a cooling medium, the cooling water is supplied into the U-tube, and the liquid used for cooling (a mixture of boiler water and steam) is discharged from the U-tube.

[0007] The carbamate liquid passed through the condenser is subjected to subsequent gas-liquid separation using a gas-liquid separator, the gaseous components are fed to the regeneration device, and the liquid components are fed to the ejector and then to the urea production reactor.

[0008] A disadvantage of the existing solution is the need for complete condensation of the supplied gases, which requires installing the heat exchanger inside the high-pressure apparatus. The apparatus is large and complex, leading to high manufacturing costs, high metal consumption, and complicated maintenance.

[0009] The closest comparable patent is EP 1170284, published on January 9, 2022, which discloses a vertical condensation and synthesis column (hereinafter referred to as the column). Condensed liquid, introduced into the upper section (synthesis section) from the condensation section (lower section) of the column, is mixed with liquid ammonia feedstock fed through a pipe in the middle of the column, thereby producing ammonium carbamate from uncondensed ammonia and carbon dioxide.

[0010] At the top of the column is the upper end of a pipe for removing the urea synthesis solution obtained in the column and entering a stripper. A liquid surface forms above the pipe opening. The portion above the liquid surface is the liquid-gas separation section, which separates inert gases (hydrogen and nitrogen contained in carbon dioxide, as well as air introduced to prevent corrosion of the apparatus) and accompanying ammonia and carbon dioxide from the urea synthesis solution.

[0011] The uppermost section of the column is equipped with a scrubber section designed to wash the gas separated in the liquid-gas separation section by absorbing ammonia and carbon dioxide in the gas with an absorbing medium, which may be a liquid containing ammonium carbamate obtained by collecting unreacted ammonia and carbon dioxide in a urea solution from the stripping column. The absorbing medium contacts the gas rising from the liquid-gas separation section, absorbing some of the ammonia and carbon dioxide, and flows down the column through a pipe. The gas is then removed through a pipe at the top of the column. The condensing section of the column is equipped with a baffle to improve liquid-gas contact.

[0012] A disadvantage of the existing solution is the need for complete condensation of the supplied gases, which requires installing a heat exchanger inside the high-pressure apparatus. This increases the size and complexity of the apparatus, leading to high manufacturing costs, high metal consumption, and complicated maintenance. The apparatus's size is increased not only by installing the heat exchanger but also by incorporating the urea production section within it. The apparatus's complexity is further increased not only by installing the heat exchanger inside the high-pressure vessel but also by injecting liquid ammonia at two points within the apparatus.

[0013] Disclosure of the essence of the utility model

[0014] The technical result of this utility model is an increase in the operating efficiency of the device, expressed in obtaining a high content of ammonium carbamate in the solution discharged from the device and ensuring the required temperature of the liquid phase at the outlet of the device while reducing the metal consumption of the device.

[0015] In order to achieve the claimed technical result, a device is proposed for separating a gas-liquid mixture containing ammonium carbamate, comprising: a housing having an upper part and a lower part, an inlet pipe for feeding the gas-liquid mixture, an outlet pipe for removing the separated liquid, an outlet pipe for removing gas, wherein mass-exchange plates are located in the lower part, the inlet pipe for feeding the gas-liquid mixture is located in the lower part under the mass-exchange plates, and the outlet pipe for removing the separated liquid is located in the lower part above the mass-exchange plates, wherein the mass-exchange plates are located at a distance H5 from each other, amounting to 0.4-1.5 times the diameter D3 of the lower part.

[0016] The location of the inlet pipe for feeding the gas-liquid mixture in the lower part under the mass-exchange plates, and the outlet pipe for removing the separated liquid in the lower part above the mass-exchange plates, as well as the location of the mass-exchange plates at the specified distance, allows for a reduction in the risk of back mixing along the flow of the gas-liquid medium (the reaction products are not mixed with the raw materials), an improvement in the alignment of the velocity profile of the gas-liquid flow, and an increase in the efficiency of the device, resulting in obtaining a high content of ammonium carbamate and the required temperature of the liquid phase at the outlet of the device in the solution removed from the device while reducing the metal consumption of the device.

[0017] Reducing the risk of backmixing during gas-liquid flow and improving the alignment of the gas-liquid flow velocity profile allows for a high content of ammonium carbamate in the solution discharged from the device with a smaller volume, which allows for the use of a smaller device with thinner walls.

[0018] Preferably, the central axis of the outlet pipe for draining the separated liquid is at a distance H7 from the outer surface of the bottom of the lower part, equal to 2-3 diameters D3 of the lower part, preferably equal to 2-2.5 diameters D3 of the lower part.

[0019] This arrangement of the outlet pipe for the discharge of separated liquid allows for an additional reduction in the risk of back-mixing during the movement of the gas-liquid medium (the reaction products are not mixed with the raw materials) and provides an additional increase in the efficiency of the device, resulting in the production of a high content of ammonium carbamate and the provision of the required temperature in the solution discharged from the device while reducing the metal consumption of the device.

[0020] Preferably, 2-5 mass transfer plates, preferably 3-4 mass transfer plates, are located in the lower part.

[0021] This number of mass-transfer trays improves the alignment of the gas-liquid flow velocity profile and provides an additional increase in the device's operating efficiency, resulting in a high ammonium carbamate content and the required temperature in the solution discharged from the device while reducing the device's metal consumption. Preferably, the mass-transfer trays are spaced at a distance H5 from each other equal to 0.5-1.0 times the diameter D3 of the lower part, preferably 0.5-0.7 times the diameter

[0022] D3 lower part.

[0023] This arrangement of mass-transfer plates allows for additional improvement in the alignment of the gas-liquid flow velocity profile and provides an additional increase in the efficiency of the device, resulting in obtaining a high content of ammonium carbamate and ensuring the required temperature in the solution discharged from the device while reducing the metal consumption of the device.

[0024] Preferably, the lower mass transfer plate is located at a distance H5i from the inner surface of the bottom of the lower part, equal to 0.5-1.5 of the diameter D3 of the lower part, preferably 0.5-1.0 of the diameter D3 of the lower part, more preferably 0.5-0.7 of the diameter D3 of the lower part.

[0025] This arrangement of mass-transfer plates allows for additional improvement in the alignment of the gas-liquid flow velocity profile and provides an additional increase in the efficiency of the device, resulting in obtaining a high content of ammonium carbamate and ensuring the required temperature in the solution discharged from the device while reducing the metal consumption of the device.

[0026] Preferably, the free cross-section of the mass transfer plate is 5-30% of the area of ​​the mass transfer plate, preferably 6-10% of the area of ​​the mass transfer plate.

[0027] This design of mass-transfer trays allows for further improvement in the alignment of the gas-liquid flow velocity profile and provides further improvement in the device's operating efficiency, resulting in high ammonium carbamate content and the required temperature in the solution discharged from the device, all while reducing the device's metal consumption. In this application, the free cross-sectional area refers to the total area of ​​the narrowest cross-section of the gas passage openings at the base of the tray.

[0028] Preferably, the mass transfer tray has downwardly directed side walls, wherein the side walls have a height H С5 , equal to 100-300 mm, preferably 150-250 mm.

[0029] Specified height H С5The side walls (flanging / bending of the plate edge downwards) allow for additional improvement in the alignment of the gas-liquid flow velocity profile by organizing the accumulation of the gas-liquid mixture and preventing its upward passage, which allows for an additional increase in the efficiency of the device, resulting in obtaining a high content of ammonium carbamate and ensuring the required temperature in the solution discharged from the device while reducing the metal consumption of the device.

[0030] In a preferred embodiment, the distance L5 from the side wall of the mass transfer plate to the inner wall of the lower part is 5-10 mm, preferably 6-8 mm.

[0031] The presence of the specified gap (distance) from the side wall of the mass transfer tray to the inner wall of the lower part allows the passage of gas above the tray to create an oxide film on the inner wall of the lower part, which protects it from corrosion, which allows for an additional increase in the efficiency of the device, expressed in obtaining a high content of ammonium carbamate and ensuring the required temperature in the solution discharged from the device while reducing the metal consumption of the device in terms of the expensive inner layer of lining steel.

[0032] Preferably, the ratio of the diameter D3 of the lower part to the height H3 of the lower part is 0.1-0.4, preferably 0.2-0.3.

[0033] This ratio of the diameters of the upper and lower parts and the height of the device allows for an additional improvement in the alignment of the velocity profile of the gas-liquid flow and provides an additional increase in the efficiency of the device, resulting in obtaining a high content of ammonium carbamate and ensuring the required temperature in the solution discharged from the device while reducing the metal consumption of the device.

[0034] Preferably, in the upper part there is a distributor for supplying liquid for irrigation, under which a packing and a plate are arranged in series, wherein the plate is equipped with a branch pipe for the passage of gas from the lower part to the upper part, a partition for limiting the passage of liquid from the upper part to the phase boundary of the lower part and a pipe for draining liquid under the mass transfer plates in the lower part.

[0035] This design of the upper part leads to an increase in the depth of the process and allows for an additional increase in the efficiency of the device, resulting in the production of a high content of ammonium carbamate and the provision of the required temperature in the solution discharged from the device while reducing the metal consumption of the device.

[0036] Preferably, the distribution device for supplying irrigation liquid is located at a distance H9 from the nozzle, equal to 0.1-0.3 of the diameter D2 of the upper part, preferably 0.15-0.25 of the diameter D2 of the upper part.

[0037] This design of the distribution device leads to an additional increase in the depth of the process and allows for an additional increase in the efficiency of the device, expressed in obtaining a high content of ammonium carbamate and ensuring the required temperature in the solution discharged from the device while reducing the metal consumption of the device.

[0038] Preferably, the distributor for supplying irrigation liquid comprises holes with a diameter D9i of 3-7 mm, preferably 4-6 mm, arranged in rows, wherein the angle β9 between two adjacent holes in a row is 45-75°, preferably 55-65°. This distributor design further increases the depth of the process and allows for further improvement in the device's operating efficiency, resulting in a high ammonium carbamate content and the required temperature in the solution discharged from the device, while reducing the device's metal consumption.

[0039] Preferably, the pipe for draining liquid into the lower part is located at a height H16 from the inner surface of the bottom of the lower part, equal to 0.2-0.6 of the diameter D3 of the lower part, preferably 0.3-0.5 of the diameter D3 of the lower part.

[0040] This allows for an additional reduction in the risk of back-mixing during the movement of the gas-liquid medium (the reaction products are not mixed with the raw materials) and provides an additional increase in the productivity of the device, resulting in the achievement of a high content of ammonium carbamate and the provision of the required temperature in the solution discharged from the device.

[0041] Preferably, there is a gas distribution device at the outlet of the inlet pipe for supplying the gas-liquid mixture.

[0042] The presence of a gas distribution device at the outlet of the inlet pipe for feeding the gas-liquid mixture leads to an additional increase in the depth of the process and allows for an additional increase in the efficiency of the device, expressed in obtaining a high content of ammonium carbamate and ensuring the required temperature in the solution discharged from the device while reducing the metal consumption of the device.

[0043] The gas distribution device may be any device known from the prior art that allows gas to be directed in different directions, for example, a perforated grate, a partition with holes, and so on.

[0044] Preferably, the mass transfer plate has holes of diameter D O5, amounting to 5-15 mm, preferably 8-10 mm, wherein the mass transfer plate has a central zone located at a distance of no more than 0.31 of the diameter D3 of the lower part from the center of the mass transfer plate, a peripheral zone located at a distance of more than 0.44 of the diameter D3 of the lower part from the center of the mass transfer plate, and an intermediate zone located between the central zone and the peripheral zone, wherein the number of openings per square decimeter in the central zone is less than the number of openings per square decimeter in the intermediate zone, and the number of openings per square decimeter in the intermediate zone is less than the number of openings per square decimeter in the peripheral zone.

[0045] This design of mass-transfer plates (increasing the number of holes of a given diameter as they move away from the center of the mass-transfer plate) allows for additional improvement in the alignment of the velocity profile of the gas-liquid flow and provides an additional increase in the productivity of the device, resulting in achieving a high content of ammonium carbamate and ensuring the required temperature in the solution discharged from the device.

[0046] Preferably, the mass transfer plate has zones Z1, Z2, Z3, Z5, Z5, wherein zone Z1 contains N Z1 holes and is located at a distance of 0-0.22 of the diameter D3 of the lower part from the center of the mass transfer plate, zone Z2 contains N Z2 holes and is located at a distance of 0.22-0.31 of the diameter D3 of the lower part from the center of the mass transfer plate, zone Z3 contains N Z3 holes and is located at a distance of 0.31-0.38 of the diameter D3 of the lower part from the center of the mass transfer plate, zone Z4 contains N Z4holes and is located at a distance of 0.38-0.44 of the diameter D3 of the lower part from the center of the mass transfer plate, zone Z5 contains N Z5 holes and is located at a distance of more than 0.44 of the diameter

[0047] D3 lower part from the center of the mass transfer plate, while the following conditions are met: N Z3 = N Z1 + N Z2 , N Z4 = N Z2 + N Z3 , N Z5 = N Z3 + N Z4 .

[0048] This design of mass-transfer plates allows for additional improvement in the alignment of the gas-liquid flow velocity profile and provides an additional increase in the device's performance, resulting in the achievement of a high content of ammonium carbamate and the provision of the required temperature in the solution discharged from the device.

[0049] Brief description of the drawings

[0050] The drawings are presented for a better understanding of the utility model, however, it will be obvious to a person skilled in the art that the disclosed utility model is not limited to the variant shown in them.

[0051] Fig. 1 shows a schematic view in longitudinal section of the claimed device;

[0052] Fig. 2 shows a sectional view along line A-A of the claimed device;

[0053] Fig. 3 shows a schematic view B in cross section of a fragment of a mass transfer plate with holes;

[0054] Fig. 4 shows a sectional view along line C-C of the claimed device;

[0055] Fig. 5 shows an enlarged local view E of the claimed device;

[0056] Fig. 6 shows a sectional view along line JJ of the claimed device.

[0057] Implementation of a utility model

[0058] The described embodiment examples are provided for illustrative purposes only. Those skilled in the art will readily recognize that other embodiments are possible without altering the essence of the utility model.

[0059] All components of the claimed device are interconnected by assembly operations and are in functional and structural unity. Fig. 1 shows a device 1 for separating a gas-liquid mixture containing ammonium carbamate (pre-reactor-separator).

[0060] The device 1 comprises a housing containing an upper part 2 and a lower part 3.

[0061] In the lower part 3 there is an inlet pipe 4 for feeding the gas-liquid mixture, mass-exchange plates 5 with holes, a hatch 6, an outlet pipe 7 for removing the separated liquid, and a level gauge 8.

[0062] The lower part has a bottom, an intermediate zone and an upper zone.

[0063] In the upper part 2 there is a distribution device 9 (pipe) for supplying liquid for irrigation, under which there is a nozzle 10 (Pall rings), a plate 11 equipped with a pipe 14 for the passage of gas from the lower part 3 to the upper part 2, a partition 15 for limiting the passage of liquid from the lower part 3 together with the gas and a pipe 16 for draining the liquid into the lower part 3.

[0064] In the upper part 2 above the distribution device 9 there is an outlet pipe 12 for gas removal and a flange 13.

[0065] The upper part has a diameter D2, height H2, the lower part 3 has a diameter D3, height H3.

[0066] The inlet pipe 4 for feeding the gas-liquid mixture is located at the bottom of the lower part 3.

[0067] The outlet pipe 7 for draining the separated liquid is located at a distance H7 from the outer surface of the bottom of the lower part 3.

[0068] Mass transfer plates 5 (3 pieces) are located at a distance H5 from each other, and the lower plate is located at a distance H51 from the inner surface of the bottom of the lower part 3.

[0069] The distribution device 9 (pipe) for supplying liquid for irrigation is located at a distance H9 from the nozzle 10.

[0070] Baffle 15 is designed like a stovepipe (shaped like the roof of a small house): it allows gas to pass through but not liquid. Baffle 15 is welded to a blind upper plate 11 (without openings). Gas bypasses the baffle and exits from under its cap, while liquid returns to the lower part.

[0071] The pipe 16 for draining the liquid into the lower part 3 has a diameter D16 and is located at a height H16 from the inner surface of the bottom of the lower part 3. Fig. 2 shows a sectional view along line A-A of the claimed device, which shows a mass transfer plate 5, made up of several sections, which can be the same for each section or different.

[0072] The mass transfer plate 5 contains holes along the perimeter for fastening to the lower part 3.

[0073] Fig. 3 shows a schematic view B in cross-section of a fragment of a mass-transfer plate 5 with holes 05 having a diameter D O5 .

[0074] Mass transfer plate 5 is conditionally divided into zones Z1, Z2, Z3, Z5, Z5.

[0075] The zones are located at the following distance from the center of the mass transfer plate 5: zone Z1 is located at a distance of no more than L z1 , zone Z2 is located at a distance of no more than L z2 and more L z1 , zone Z3 is located at a distance of no more than Lz3 and more L z2 , zone Z4 is located at a distance of no more than L z4 and more than Lz3, zone Z5 is located at a distance of more than L z4 .

[0076] The holes in the zones of the plate are arranged according to the "golden section" rule: zone Z1 contains N Z1 holes, zone Z2 contains N z2 holes, zone Z3 contains N Z3 holes, where N Z3 = N Z1 + N z2 , zone Z4 contains N z4 holes, where N z4 = N z2 + N Z3 , zone Z5 contains N Z5 holes, where N Z5 = N Z3 + N z4 .

[0077] Fig. 4 shows a sectional view along line C-C of the claimed device.

[0078] In particular, an enlarged view of the side wall (flanging / downward bend of the plate edge) of the mass transfer plate 5 is shown. The height of the side walls of the sections of the mass transfer plate is H С5The distance from the side wall of the mass transfer plate to the inner wall of the lower part is L5

[0079] Fig. 5 shows an enlarged local view E of the claimed device.

[0080] In particular, a section of the distribution device 9 (pipe) for supplying liquid for irrigation of length L9i is shown, on which openings 9i are located.

[0081] Fig. 6 shows a sectional view along line JJ of the claimed device.

[0082] In particular, a cross-section of a section of the distribution device 9 (pipe) for supplying liquid for irrigation of length L9i is shown, on which openings 9i are located

[0083] The openings 9i have a diameter D9i and are located in the lower part of the distribution device 9 at an angle β9 to each other.

[0084] The claimed device operates as follows.

[0085] A gas-liquid mixture from a carbamate condenser (not shown), containing ammonium carbamate, at a temperature of 160-170°C is directed through an inlet pipe 4 for a gas-liquid mixture to the lower part 3 of a device 1 for separating a gas-liquid mixture containing ammonium carbamate.

[0086] Here, the uncondensed gas phase condenses to form an additional amount of carbamate, heating the solution.

[0087] The gas-liquid mixture passes through mass-exchange plates 5 from bottom to top, the conditions in device 1 allow some of the carbamate to be converted into urea.

[0088] The liquid solution of carbamate and urea leaves the device 1 through the outlet pipe 7 for separated liquid, is directed to the high-pressure ejector and is fed to the urea synthesis reactor using a flow of liquid ammonia.

[0089] Uncondensed gases from the lower part 3 of the device 1 enter the upper part 2 through a pipe 14 built into the plate 11, which has openings for the passage of gas, while a partition 15 welded to the pipe 14 limits the passage of liquid from the lower part 3.

[0090] The gases from the lower part 3, passing through the nozzle 10, irrigated by means of the distribution device 9 (pipe) for supplying the irrigating liquid (medium pressure carbamate solution), are subject to additional condensation.

[0091] The remaining gases are discharged through the outlet pipe 12 for gas from the upper part 2, throttled to a pressure of 2.3 - 2.7 MPa and sent to the inter-tube space of the recuperative heater of the urea solution (not shown).

[0092] The carbamate solution obtained in the upper part 2 of device 1 is collected on plate 11 and drained into the lower part 3 of device 1 through pipe 16 for draining liquid.

[0093] The pressure of 14.0-14.5 MPa in device 1 is maintained by a valve on the gas outlet pipe 12.

[0094] The use of the claimed device enables increased operational efficiency, resulting in high ammonium carbamate content and the required temperature in the solution discharged from the device, while reducing the device's metal consumption. The claimed device promotes uniform distribution of the medium within the column, reduces internal flow turbulence, and improves heat and mass transfer through more precise regulation of temperature, pressure, and solution flow patterns in the intermediate (middle) section of the device, where the liquid product is withdrawn for subsequent feeding to the urea synthesis reactor. This ultimately leads to a significant increase in device productivity.

[0095] Furthermore, the proposed device of this design allows for temperature control in the urea synthesis reactor. Fine-tuning this temperature allows for increased conversion of the feedstock (carbon dioxide) into the finished product (urea). The device allows for precise setting of the optimal temperature in the upper section of the synthesis reactor, from 183 to

[0096] 192°C, preferably 185-189°C. The increase in the degree of conversion of carbon dioxide to urea in this case, compared to a scheme without the possibility of fine-tuning the temperature, is 0.5-2%.

[0097] The test results of the claimed device are presented in Table 1 below. Table 1

[0098]

[0099] Thus, the claimed utility model ensured an increase in the efficiency of the device, expressed in obtaining a high content of ammonium carbamate in the solution discharged from the device and ensuring the required temperature of the liquid phase at the outlet of the device while reducing the metal consumption of the device.

Claims

Utility model formula 1. A device for separating a gas-liquid mixture containing ammonium carbamate, comprising: a housing having an upper part and a lower part, an inlet pipe for feeding the gas-liquid mixture, an outlet pipe for removing separated liquid, an outlet pipe for removing gas, wherein mass-exchange plates are located in the lower part, the inlet pipe for feeding the gas-liquid mixture is located in the lower part under the mass-exchange plates, and the outlet pipe for removing separated liquid is located in the lower part above the mass-exchange plates, characterized in that the mass-exchange plates are located at a distance H5 from each other, which is 0.4-1.5 times the diameter D3 of the lower part.

2. The device according to item 1, characterized in that the central axis of the outlet pipe for draining the separated liquid is located at a distance H7 from the outer surface of the bottom of the lower part, equal to 2-3 diameters D3 of the lower part, preferably equal to 2-2.5 diameters D3 of the lower part.

3. The device according to item 1, characterized in that 2-5 mass transfer plates, preferably 3-4 mass transfer plates, are located in the lower part.

4. The device according to claim 1, characterized in that the mass transfer plates are located at a distance H5 from each other, which is 0.5-1.0 times the diameter D3 of the lower part, preferably 0.5-0.7 times the diameter D3 of the lower part.

5. The device according to claim 1, characterized in that the lower mass transfer plate is located at a distance H5i from the inner surface of the bottom of the lower part, equal to 0.5-1.5 times the diameter D3 of the lower part, preferably 0.5-1.0 times the diameter D3 of the lower part, more preferably 0.5-0.7 times the diameter D3 of the lower part.

6. The device according to item 1, characterized in that the free cross-section of the mass transfer plate is 5-30% of the area of ​​the mass transfer plate, preferably 6-10% of the area of ​​the mass transfer plate.

7. The device according to item 1, characterized in that the mass transfer plate has downward-directed side walls, wherein the side walls have a height H С5 , equal to 100-300 mm, preferably 150-250 mm.

8. The device according to item 1, characterized in that the distance L5 from the side wall of the mass transfer plate to the inner wall of the lower part is 5-10 mm, preferably 6-8 mm.

9. The device according to item 1, characterized in that the ratio of the diameter D3 of the lower part to the height H3 of the lower part is 0.1-0.4, preferably 0.2-0.

3.

10. The device according to claim 1, characterized in that in the upper part there is a distribution device for supplying liquid for irrigation, under which a packing and a plate are arranged in series, wherein the plate is equipped with a branch pipe for the passage of gas from the lower part to the upper part, a partition for limiting the passage of liquid from the upper part to the phase boundary of the lower part, and a pipe for draining liquid under the mass-transfer plates in the lower part. I. The device according to I. 10, characterized in that the distribution device for supplying liquid for irrigation is located at a distance H9 from the nozzle, equal to 0.1-0.3 of the diameter D2 of the upper part, preferably 0.15-0.25 of the diameter D2 of the upper part.

12. The device according to item 10, characterized in that the distribution device for supplying liquid for irrigation contains openings with a diameter D9i of 3-7 mm, preferably 4-6 mm, arranged in rows, wherein the angle β9 between two adjacent openings in one row is 45-75°, preferably 55-65°.

13. The device according to item 10, characterized in that the pipe for draining liquid into the lower part is located at a height H16 from the inner surface of the bottom of the lower part, equal to 0.2-0.6 of the diameter D3 of the lower part, preferably 0.3-0.5 of the diameter D3 of the lower part.

14. The device according to paragraph 1, characterized in that at the outlet of the inlet pipe for supplying the gas-liquid mixture there is a gas distribution device.

15. The device according to item 1, characterized in that the mass transfer plate has holes of diameter D O5, amounting to 5-15 mm, preferably 8-10 mm, wherein the mass transfer plate has a central zone located at a distance of no more than 0.31 of the diameter D3 of the lower part from the center of the mass transfer plate, a peripheral zone located at a distance of more than 0.44 of the diameter D3 of the lower part from the center of the mass transfer plate, and an intermediate zone located between the central zone and the peripheral zone, wherein the number of openings per square decimeter in the central zone is less than the number of openings per square decimeter in the intermediate zone, and the number of openings per square decimeter in the intermediate zone is less than the number of openings per square decimeter in the peripheral zone.

16. The device according to item 1, characterized in that the mass transfer plate has zones Z1, Z2, Z3, Z5, Z5, wherein zone Z1 contains N Z1 holes and is located at a distance of 0-0.22 of the diameter D3 of the lower part from the center of the mass transfer plate, zone Z2 contains N z2holes and is located at a distance of 0.22-0.31 of the diameter D3 of the lower part from the center of the mass transfer plate, zone Z3 contains N z3 holes and is located at a distance of 0.31-0.38 of the diameter D3 of the lower part from the center of the mass transfer plate, zone Z4 contains N z4 holes and is located at a distance of 0.38-0.44 of the diameter D3 of the lower part from the center of the mass transfer plate, zone Z5 contains N Z5 holes and is located at a distance of more than 0.44 of the diameter D3 lower part from the center of the mass transfer plate, while the following conditions are met: N Z3 = N Z1 + N Z2 , N Z4 = N Z2 + N Z3 , N Z5 = N Z3 + N Z4 .

Images