CN114433001B - Tandem type high-speed spin flow gas-liquid mass transfer system - Google Patents
Tandem type high-speed spin flow gas-liquid mass transfer system Download PDFInfo
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- CN114433001B CN114433001B CN202011197805.1A CN202011197805A CN114433001B CN 114433001 B CN114433001 B CN 114433001B CN 202011197805 A CN202011197805 A CN 202011197805A CN 114433001 B CN114433001 B CN 114433001B
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- 239000007788 liquid Substances 0.000 title claims abstract description 174
- 238000000926 separation method Methods 0.000 claims abstract description 83
- 239000007921 spray Substances 0.000 claims abstract description 49
- 238000000034 method Methods 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 5
- 230000000630 rising effect Effects 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 5
- 239000012071 phase Substances 0.000 description 9
- 239000010410 layer Substances 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 5
- 230000001174 ascending effect Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000011229 interlayer Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
- B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a serial high-speed spin flow gas-liquid mass transfer system. The gas-liquid mass transfer system consists of a plurality of groups of tower plate components, tower plates and a shell, wherein the shell comprises the plurality of groups of tower plate components and a plurality of tower plates; each group of tray components consists of a plurality of tray components connected in series, and each tray component comprises a gas-liquid separation pipe, a bottom plate, a downcomer, a hollow spiral plate spray head, a ring plate, a liquid inlet pipe and a double-spiral structure cap. The system strengthens the gas-liquid mass transfer effect, reduces the tower diameter tower height and improves the gas-liquid mass transfer efficiency.
Description
Technical Field
The invention relates to the technical field of gas-liquid intensified mass transfer and energy saving, in particular to a serial high-speed spin flow gas-liquid mass transfer system.
Background
Along with the continuous expansion and upgrading of petrochemical production devices, the throughput and the volume of the production devices are continuously increased, wherein the towers are particularly important equipment in the petrochemical production devices. The large-diameter tower equipment not only increases the difficulty of equipment transportation and field installation, but also greatly increases equipment investment. Therefore, the development of the efficient and high-flux gas-liquid mass transfer tower and the tower tray has great significance.
The I type large flux tower plates at home and abroad increase the effective gravity coefficient by reducing resistance, on one hand, the jet type tower plates are adopted to reduce the pressure drop between the plates, such as tongue type tower plates, mesh type tower plates and the like; on the other hand, resistance is reduced by changing the downcomer structure or gas-liquid contacting elements. The principle of the domestic and foreign class II large-flux tower plates is that the gravity field force is increased by centrifugal force, and the treatment capacity and effect of the tower plates are improved by introducing a centrifugal contact and separation device. Such as Con-Sep trays developed by Shell company, co-Flo trays developed by Jager company, etc., and after the mass transfer of these trays is intensified by centrifugal force, a great deal of entrainment phenomenon exists, and how to efficiently separate gas from liquid is a technical disadvantage of the trays.
Patent CN104959106B discloses a gas-lift cyclone liquid suction and liquid drop isolated column plate, which belongs to the technical field of contact type gas-liquid mass transfer. The mechanism and appearance are similar to those of common tower plates, but have obvious difference. Firstly, the invention adds a liquid inlet and liquid storage interlayer for isolating gas phase, thereby completely avoiding the problem of 'flooding' caused by the high-speed gas phase ascending flow lifting liquid phase in the conventional tower plate and the descending resistance of the liquid phase. Secondly, a group of rotational flow guide vanes are fixedly arranged in each channel of the gas phase ascending flow, so that the ascending gas phase rotates at a high speed to generate a centrifugal force field: on one hand, the liquid phase is sucked from the central low-pressure area, so that the circulating flow of the liquid phase is smoother; on the other hand, the sucked liquid phase is torn into countless fine fog drop particles under the shearing action of the angular velocity difference between the gas phase rotation 'combined vortex', so that the specific surface area contacted with the gas phase is greatly increased, and the gas-liquid mass transfer efficiency is improved; meanwhile, the formed fog drops are efficiently separated by the high-speed rotating flow field, so that entrainment phenomenon is avoided. The invention can doubly promote the gas flow velocity in the tower, reduce the tower diameter and improve the unit volume efficiency of the equipment. However, the wall of the gas phase riser is provided with a plurality of wall holes, the treated gas can enter the space between the tower plates through the wall holes to form vortex so as to increase the resistance of the tower plates, the gas can only flow to the top of the tower through the gas phase riser, the gas can not be distributed among the tower plates again, and the drift problem of the gas in the tower can exist.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a serial high-speed spin flow gas-liquid mass transfer system. The system strengthens the gas-liquid mass transfer effect, reduces the tower diameter tower height and improves the gas-liquid mass transfer efficiency by arranging a static cyclone component, a high-efficiency gas-liquid separation component and the like. The system has the characteristics of safety, reliability, simple equipment and operation, low investment cost and the like.
The invention provides a serial high-speed spin flow gas-liquid mass transfer system, which consists of a plurality of groups of tower plate components, tower plates and a shell, wherein the shell comprises the plurality of groups of tower plate components and the plurality of tower plates; each group of tray components consists of a plurality of tray components connected in series, and each tray component comprises a gas-liquid separation pipe, a bottom plate, a downcomer, a hollow spiral plate spray head, a ring plate, a liquid inlet pipe and a double-spiral structure cap;
the tower plate components are connected in series end to form a group of tower plate components, when two adjacent tower plate components are connected, gas-liquid separation pipes of the two tower plate components are welded and fixed, and a double-spiral structural cap of the lower tower plate component is welded and fixed with the tail end of a hollow double-spiral spray head of the upper tower plate component.
The gas-liquid separation pipe penetrates through the tower plate; the middle lower part of the gas-liquid separation pipe is provided with a hollow spiral plate spray head, the middle lower part of the hollow spiral plate spray head is provided with a ring plate, and the line contact part of the ring plate and the hollow spiral plate spray head is welded and fixed; the lower end of the gas-liquid separation tube is provided with a circular bottom plate, the outer edge of the bottom plate is welded with the bottom of the gas-liquid separation tube, and the inner edge of the bottom plate is welded and fixed with the outer wall of the annular plate.
The hollow spiral plate spray head is in a spiral plate shape, the inside of the hollow spiral plate spray head is in a hollow structure, one end of the liquid inlet pipe is connected with a liquid inlet at the top end of the hollow spiral plate spray head, and the other end, namely the inlet end, extends to the upper part of the adjacent tower plate through the pipe wall of the gas-liquid separation pipe; the outer surface of the spiral plate of the hollow spiral plate spray head is uniformly provided with a plurality of small holes and fins, the small holes are communicated with the liquid inlet pipe, the fins are fixedly welded with the outer surface of the spiral plate, and the open area of the small holes is smaller than or equal to the sectional area of the liquid inlet pipe.
The liquid inlet at the upper end of the downcomer is arranged at the lower part of the gas-liquid separation pipe, and the height of the liquid inlet from the bottom plate is generally 0-20 mm, preferably 5-10 mm. The liquid outlet at the lower end of the downcomer extends to the upper part of the adjacent lower tray, and the height from the tray is 10-40 mm, preferably 20-30 mm. And the lower end of the downcomer is lower than the liquid inlet of the liquid inlet pipe of the lower tower plate component, preferably 10-20 mm lower, and the caliber of the downcomer is DN 15-DN 50 stainless steel pipe.
Further, the inlet end of the liquid inlet pipe passes through the gas-liquid separation pipe and is fixed on the gas-liquid separation pipe, the liquid inlet pipe is placed on the column plate and is fixedly connected with the column plate, and the inlet of the liquid inlet pipe is upward.
In the invention, the small holes arranged on the hollow spiral plate spray head are preferably round holes, and the diameters of the round holes are generally 1-3 mm, preferably 1-2 mm.
In the invention, the shape of the fin arranged on the hollow spiral plate spray head is preferably round, semicircular or elliptic, and the diameter of the fin is generally 2-8 mm, preferably 3-5 mm.
In the invention, the number of the fins on the hollow spiral plate spray head is equal to or less than the number of the small holes.
In the invention, the inner wall of the gas-liquid separation pipe is provided with a plurality of separation components. The height of the separation member is consistent with that of the gas-liquid separation pipe, the separation member is preferably spiral, the contact part of the separation member and the gas-liquid separation pipe is welded and fixed, the thickness of the separation member is generally 1-2 mm, the width of the separation member is generally 5-100 mm, and a plurality of fins are preferably arranged on the surface of the separation member.
The working principle of the serial high-speed spin flow gas-liquid mass transfer system of the invention is as follows: the liquid on the upper layer of tower plate enters the hollow spiral plate spray head through the liquid inlet pipe and flows out through the small holes on the surface of the hollow spiral plate spray head. The liquid is sheared and atomized by the gas rising spirally on the surface of the spiral spray head, and mass transfer process occurs. The atomized liquid moves upwards along the spiral flow channel along with the airflow, and sequentially hits the fins on the outer surface of the hollow spiral plate spray head, the inner wall of the gas-liquid separation tube, the upper separation member of the gas-liquid separation tube and the double-spiral structure cap, so that the flow speed and the flow direction of the gas carrying the atomized liquid are continuously changed suddenly. The change in flow rate and direction of the gas reduces the carrying capacity of the gas for the atomized liquid contained therein, so that the atomized droplets are captured at the junction of the separation member and the gas-liquid separation tube and continue to coalesce until flowing down the inner wall of the gas-liquid separation tube. The separation of atomized liquid and gas is realized through the fins, the separation members and the double-spiral structural caps, the gas-liquid mass transfer is further enhanced in the gas-liquid separation process, the liquid separated by the gas-liquid separation tube is aggregated into liquid flow, and then the liquid flows to the next layer of tower plates through the downcomer, and the process is continuously and circularly carried out in a plurality of groups of tower plate members connected in series.
Compared with the prior art, the serial high-speed spin flow gas-liquid mass transfer system has the following advantages:
1. in the serial high-speed spin-flow gas-liquid mass transfer system, liquid passes through the hollow spiral plate spray head, the gas-liquid separation tube and the double-spiral structure cap to strengthen mass transfer for many times, so that the gas-liquid mass transfer and separation effect are strengthened, and the mass transfer efficiency of the tower plate is effectively improved. Under the condition of increasing the gas velocity, the invention has more obvious mass transfer strengthening effect, can effectively reduce the space between tower plates and the tower diameter, and reduces the investment of the tower.
2. In the serial high-speed spin flow gas-liquid mass transfer system, liquid is separated from gas through the gas-liquid separation pipe and then flows automatically to the next layer of tower plate through the downcomer, when the liquid and the gas pass through the upper layer of tower plate and the lower layer of tower plate, the gas-liquid two phases are not in direct contact, and the gas-liquid entrainment phenomenon caused by the lifting action of ascending gas on descending liquid can be effectively avoided.
3. In the serial high-speed spin flow gas-liquid mass transfer system, each group of tower plate components is formed by connecting a plurality of tower plate components in series, and the corresponding open holes of the tower plate components on each layer of tower plate are the same in position, so that the space in the tower can be fully and effectively utilized. Under the condition of increasing the gas quantity, the treatment capacity can be improved by increasing the number of column plate component groups, the tower diameter can be effectively reduced, and the investment of the tower can be reduced.
Drawings
Fig. 1 is a schematic diagram of the overall structure of a tandem high-speed spin-flow gas-liquid mass transfer system of the present invention.
FIG. 2 is a schematic representation of the structure of a single tray member of the present invention.
FIG. 3 is a schematic view of the structure of the gas-liquid separation tube and the inner wall separation member thereof according to the present invention.
FIG. 4 is a schematic view of the structure of the partial openings and fins of the hollow spiral plate spray head of the present invention.
The device comprises a 1-shell, a 2-tower plate, a 3-tower plate component, a 4-bottom plate, a 5-downcomer, a 6-hollow spiral plate spray head, a 7-liquid inlet pipe, an 8-double spiral structure cap, a 9-gas-liquid separation pipe, 10-small holes, 11-separation components, 12-annular plates and 13-fins.
Detailed Description
The present invention will be further illustrated by the following examples, but is not limited to the examples.
In the description of the present invention, it should be noted that the positional or positional relationship indicated by the terms such as "upper", "lower", "inner", "outer", "top", "bottom", etc. are based on the positional or positional relationship shown in the drawings, are merely for convenience of describing the present invention and simplifying the description, and do not indicate or imply that the apparatus or element in question must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless explicitly stated and limited otherwise, the terms "provided with," "disposed," "connected," "mounted," etc. are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
As shown in FIG. 1, the invention provides a serial high-speed spin-flow gas-liquid mass transfer system. The gas-liquid mass transfer system consists of a plurality of groups of column plate members 3, column plates 2 and a shell 1. The shell 1 comprises a plurality of groups of tray components 3 and a plurality of trays 2; each group of tray components 3 is composed of a plurality of tray components 3 connected in series, and each tray component 3 comprises a gas-liquid separation pipe 9, a bottom plate 4, a downcomer 5, a hollow spiral plate spray head 6, a ring plate 12, a liquid inlet pipe 7 and a double spiral structure cap 8.
The plurality of tray components 3 are connected end to end and connected in series to form a group of tray components. When two adjacent tower plate components 3 are connected, gas-liquid separation pipes 9 of the two are welded and fixed, and a double-spiral structure cap 8 of the lower tower plate component 3 is welded and fixed with the tail end of a hollow double-spiral spray head of the upper tower plate component 3.
The gas-liquid separation pipe 9 penetrates through the column plate 2. The middle lower part of the gas-liquid separation pipe 9 is provided with a hollow spiral plate spray head 6. The middle lower part of the hollow spiral plate spray head 6 is provided with a ring plate 12, and the ring plate 12 is welded and fixed at the line contact part of the hollow spiral plate spray head 6. The lower end of the gas-liquid separation tube 9 is provided with a circular bottom plate 4, the outer edge of the bottom plate 4 is welded with the bottom of the gas-liquid separation tube 9, and the inner edge of the bottom plate 4 is welded and fixed with the outer wall of the annular plate 12.
The hollow spiral plate spray head 6 is in a spiral plate shape, and the inside of the hollow spiral plate spray head is in a hollow structure. One end of the liquid inlet pipe 7 is connected with a liquid inlet at the top end of the hollow spiral plate spray head 6, and the other end, namely the inlet end, penetrates through the pipe wall of the gas-liquid separation pipe 9 and extends to the upper part of the adjacent tower plate 2. The outer surface of the spiral plate of the hollow spiral plate spray head 6 is uniformly provided with a plurality of small holes 10 and fins 13, and the small holes 10 are communicated with the liquid inlet pipe 7. The fins 13 are welded and fixed with the outer surface of the spiral plate, and the open area of the small holes 10 is smaller than or equal to the sectional area of the liquid inlet pipe 7.
The liquid inlet at the upper end of the downcomer 5 is arranged at the lower part of the gas-liquid separation pipe 9, and the height from the bottom plate 4 is generally 0-20 mm, preferably 5-10 mm. The liquid outlet at the lower end of the downcomer 5 extends to the upper part of the adjacent lower tray 2, and the height from the tray 2 is 10-40 mm, preferably 20-30 mm. The lower end of the downcomer 5 is lower than the liquid inlet of the liquid inlet pipe 7 of the lower tower plate member 3, preferably 10-20 mm lower, and the caliber of the downcomer 5 is DN 15-DN 50 stainless steel pipe.
Further, the inlet end of the liquid inlet pipe 7 passes through the gas-liquid separation pipe 9 and is fixed on the gas-liquid separation pipe 9, the liquid inlet pipe 7 is placed on the column plate 2 and is fixedly connected with the column plate 2, and the inlet of the liquid inlet pipe 7 is upward.
In the invention, the small holes 10 arranged on the hollow spiral plate spray head 6 are preferably round holes, and the diameter of the round holes is generally 1-3 mm, preferably 1-2 mm.
In the invention, the shape of the fin 13 arranged on the hollow spiral plate spray head 6 is preferably circular, semicircular or elliptic, and the diameter of the fin 13 is generally 2-8 mm, preferably 3-5 mm.
In the invention, the number of the fins 13 on the hollow spiral plate spray head 6 is equal to or less than the number of the small holes 10.
In the present invention, the inner wall of the gas-liquid separation tube 9 is provided with a plurality of separation members 11. The height of the separating member 11 is consistent with that of the gas-liquid separating pipe 9, the separating member 11 is preferably spiral, the part in line contact with the gas-liquid separating pipe 9 is welded and fixed, the thickness of the separating member 11 is generally 1-2 mm, the width of the separating member 11 is generally 5-100 mm, and a plurality of fins are preferably arranged on the surface of the separating member 11.
The working principle of the serial high-speed spin flow gas-liquid mass transfer system of the invention is as follows: the liquid on the upper layer of tower plate 2 enters the hollow spiral plate spray head 6 through the liquid inlet pipe 7 and flows out through the small holes 10 on the surface of the hollow spiral plate spray head 6. The liquid is sheared and atomized by the gas rising spirally on the surface of the spiral spray head, and mass transfer process occurs. The atomized liquid moves upwards along the spiral flow channel along with the airflow, and sequentially hits the fins 13 on the outer surface of the hollow spiral plate spray head 6, the inner wall of the gas-liquid separation tube 9, the upper separation member 11 of the gas-liquid separation tube and the double-spiral structural cap 8, so that the flow speed and the flow direction of the gas carrying the atomized liquid are continuously changed suddenly. The change in the flow rate and flow direction of the gas reduces the carrying capacity of the gas for the atomized liquid contained therein, so that the atomized droplets are captured at the junction of the separation member 11 and the gas-liquid separation tube 9 and continue to coalesce until flowing down the inner wall of the gas-liquid separation tube 9. The separation of atomized liquid and gas is realized through the fins 13, the separation members 11 and the double-spiral structural cap 8, the gas-liquid mass transfer is further enhanced in the gas-liquid separation process, the liquid separated by the gas-liquid separation tube 9 is aggregated into a liquid flow, and then the liquid flows onto the next layer of tower plate 2 through the downcomer 5, and the process is continuously circulated in a plurality of groups of tower plate members 3 connected in series.
Claims (10)
1. The serial high-speed spin flow gas-liquid mass transfer system is characterized by comprising a plurality of groups of column plate components, column plates and a shell;
the shell comprises a plurality of groups of tower plate components and a plurality of tower plates; each group of tray components consists of a plurality of tray components connected in series, and each tray component comprises a gas-liquid separation pipe, a bottom plate, a downcomer, a hollow spiral plate spray head, a ring plate, a liquid inlet pipe and a double-spiral structure cap;
the plurality of column plate components are connected end to form a group of column plate components;
when two adjacent tower plate components are connected, gas-liquid separation pipes of the two tower plate components are welded and fixed, and a double-spiral structural cap of a lower tower plate component is welded and fixed with the tail end of a hollow double-spiral spray head of an upper tower plate component;
the gas-liquid separation pipe penetrates through the tower plate;
the middle lower part of the gas-liquid separation pipe is provided with a hollow spiral plate spray head, the middle lower part of the hollow spiral plate spray head is provided with a ring plate, and the joint of the ring plate and the hollow spiral plate spray head in line contact is welded and fixed;
the lower end of the gas-liquid separation tube is provided with a circular bottom plate, the outer edge of the bottom plate is welded with the bottom of the gas-liquid separation tube, and the inner edge of the bottom plate is welded and fixed with the outer wall of the annular plate;
the hollow spiral plate spray head is in a spiral plate shape, the inside of the hollow spiral plate spray head is in a hollow structure, one end of the liquid inlet pipe is connected with a liquid inlet at the top end of the hollow spiral plate spray head, and the other end, namely the inlet end, extends to the upper part of the adjacent tower plate through the pipe wall of the gas-liquid separation pipe; the liquid inlet at the upper end of the downcomer is arranged at the lower part of the gas-liquid separation pipe, and the liquid outlet at the lower end of the downcomer extends to the upper part of the adjacent lower tower plate;
the liquid on the upper layer of tower plate enters the hollow spiral plate spray head through the liquid inlet pipe, flows out through the small holes on the surface of the hollow spiral plate spray head, is sheared and atomized by the gas rising spirally on the surface of the spiral spray head, and generates a mass transfer process, the atomized liquid moves upwards along the spiral flow channel along with the gas flow, sequentially impacts the fins on the outer surface of the hollow spiral plate spray head, the inner wall of the gas-liquid separation pipe and the double-spiral structure cap, finally realizes the separation of the atomized liquid and the gas, further strengthens the gas-liquid mass transfer in the gas-liquid separation process, and the liquid separated by the gas-liquid separation pipe is aggregated into liquid flow, and then flows to the next layer of tower plate through the downcomer.
2. The gas-liquid mass transfer system according to claim 1, wherein a plurality of small holes and fins are uniformly arranged on the outer surface of the spiral plate of the hollow spiral plate spray head, the small holes are communicated with the liquid inlet pipe, and the fins are welded and fixed on the outer surface of the spiral plate.
3. The gas-liquid mass transfer system of claim 2, wherein the open area of the plurality of apertures is less than or equal to the cross-sectional area of the feed tube.
4. The gas-liquid mass transfer system of claim 1, wherein the lower end of the downcomer is below the liquid inlet of the liquid inlet pipe of the lower adjacent tray member.
5. The gas-liquid mass transfer system of claim 1, wherein the inlet end of the liquid inlet tube passes through the gas-liquid separation tube and is fixed to the gas-liquid separation tube, and the liquid inlet tube is disposed on and fixedly connected to the tray with the inlet of the liquid inlet tube facing upward.
6. The gas-liquid mass transfer system of claim 2, wherein said apertures are circular holes and said fins are circular, semi-circular or oval.
7. The gas-liquid mass transfer system of claim 2, wherein the number of fins on said hollow spiral plate nozzle is equal to or less than the number of small holes.
8. The gas-liquid mass transfer system according to claim 1, wherein the inner wall of the gas-liquid separation tube is provided with a plurality of separation members, and the height of the separation members is identical to the height of the gas-liquid separation tube.
9. The gas-liquid mass transfer system of claim 8, wherein said separation member is spiral in shape and is welded in place in contact with the gas-liquid separation line.
10. The gas-liquid mass transfer system of claim 9, wherein a plurality of fins are provided on a surface of the separation member.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011197805.1A CN114433001B (en) | 2020-10-31 | 2020-10-31 | Tandem type high-speed spin flow gas-liquid mass transfer system |
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| CN202011197805.1A CN114433001B (en) | 2020-10-31 | 2020-10-31 | Tandem type high-speed spin flow gas-liquid mass transfer system |
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| CN114433001A CN114433001A (en) | 2022-05-06 |
| CN114433001B true CN114433001B (en) | 2023-10-10 |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104014096A (en) * | 2014-06-20 | 2014-09-03 | 武汉科技大学 | Direct-through double-helix convergent type water pressure atomizing spray nozzle |
| CN104941246A (en) * | 2015-04-21 | 2015-09-30 | 昆明理工大学 | Impinging stream super-gravity liquid-liquid extractor |
| CN104959106A (en) * | 2015-07-13 | 2015-10-07 | 大连理工大学 | Air-lift cyclone liquid absorption and liquid falling isolation-type tower plate |
| CN109985576A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of gas-liquid mass transfer system |
| CN209378725U (en) * | 2018-08-29 | 2019-09-13 | 浙江易澄环保科技有限公司 | A kind of Multi-stage spiral-plate tower |
| CN210171454U (en) * | 2019-03-21 | 2020-03-24 | 通辽金煤化工有限公司 | Pipeline gas-liquid mixing device for producing coal-to-ethylene glycol |
| CN111617635A (en) * | 2020-06-16 | 2020-09-04 | 浙江天地环保科技股份有限公司 | Novel denitration reductant directly spout and mix device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5621104B2 (en) * | 2010-09-02 | 2014-11-05 | 株式会社エプシロン | Regular packing for gas-liquid contactor |
-
2020
- 2020-10-31 CN CN202011197805.1A patent/CN114433001B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104014096A (en) * | 2014-06-20 | 2014-09-03 | 武汉科技大学 | Direct-through double-helix convergent type water pressure atomizing spray nozzle |
| CN104941246A (en) * | 2015-04-21 | 2015-09-30 | 昆明理工大学 | Impinging stream super-gravity liquid-liquid extractor |
| CN104959106A (en) * | 2015-07-13 | 2015-10-07 | 大连理工大学 | Air-lift cyclone liquid absorption and liquid falling isolation-type tower plate |
| CN109985576A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of gas-liquid mass transfer system |
| CN209378725U (en) * | 2018-08-29 | 2019-09-13 | 浙江易澄环保科技有限公司 | A kind of Multi-stage spiral-plate tower |
| CN210171454U (en) * | 2019-03-21 | 2020-03-24 | 通辽金煤化工有限公司 | Pipeline gas-liquid mixing device for producing coal-to-ethylene glycol |
| CN111617635A (en) * | 2020-06-16 | 2020-09-04 | 浙江天地环保科技股份有限公司 | Novel denitration reductant directly spout and mix device |
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| CN114433001A (en) | 2022-05-06 |
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Effective date of registration: 20231214 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |