CN111013178B - Stepped liquid circulation bubble tower and method for dispersing gas - Google Patents
Stepped liquid circulation bubble tower and method for dispersing gas Download PDFInfo
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- CN111013178B CN111013178B CN201911302733.XA CN201911302733A CN111013178B CN 111013178 B CN111013178 B CN 111013178B CN 201911302733 A CN201911302733 A CN 201911302733A CN 111013178 B CN111013178 B CN 111013178B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
- B01D3/24—Fractionating columns in which vapour bubbles through liquid with sloping plates or elements mounted stepwise
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
Abstract
The invention discloses a stepped liquid circulation bubbling tower and a method for dispersing gas. The semicircular tower plate is horizontally fixed on the inner side of the tower wall and the central partition plate, and is provided with a plurality of specially-made bubbling elements. The stepped liquid circulating bubbling tower and the special bubbling element make liquid flow circularly downwards alternately on the tower plates on two sides of the central partition board, and the present invention has the advantages of stable gas dispersion, high gas-liquid mass transfer driving force, etc. and is suitable for application in gas-liquid mass transfer separation, gas-liquid reaction, etc.
Description
Technical Field
The invention relates to a stepped liquid circulation bubble column, which can be used for unit operations such as rectification, absorption, gas-liquid reaction and the like in a chemical process, and particularly provides a gas dispersion method with larger operation flexibility and high efficiency for high liquid-gas ratio operation processes such as extraction rectification, reactive rectification and the like.
Background
For a conventional plate-type rectification column, most of liquid in the column is confined in a small space on a plate, a large space above the plate is filled with a gas phase, and only a small part of liquid is dispersed in the gas phase as mist. Although the mass transfer efficiency of most of the tower plates is not low, the space utilization rate is low due to serious uneven liquid distribution. The appearance of the high-efficiency filler greatly improves the space utilization rate of the rectifying tower, but the quality requirements on the filler and the distributor in the tower body with larger diameter are very high, and the due separation efficiency of the filler and the distributor cannot be achieved in production.
In chemical production, there are special separation processes, such as extractive distillation and reactive distillation, and the characteristic is that the liquid-gas ratio in operation is very large, the variation range of gas flow is large in the whole separation process, and the tower plate with a single structure is difficult to adapt to different gas flow conditions. And a smaller gas flow may only be required with a small diameter tray, which is also contradictory to a correspondingly larger liquid flow or longer residence time. As for the packed column, a large liquid amount requires a large column diameter, and it is also liable that a gas of a small flow rate is hardly uniformly distributed.
A filler foam filling tower which takes a liquid phase as a continuous phase is also called an emulsifying tower in the chemical production in the seventies of the last century. The equipment is used for the rectification process to obtain higher separation efficiency, but because the tower type has higher requirements on gas-liquid flow distribution, the tower type is mostly limited to occasions with the tower diameter less than 600mm, and no application report of a large-scale rectification tower is seen.
The invention provides a stepped liquid circulation bubble tower structure aiming at the separation operation of large liquid-gas ratio, and is combined with a special bubble element for gas dispersion and gas-liquid mass transfer processes. The hydraulics experiment shows that the arrangement mode of the alternate tower plates on two sides of the central partition plate can promote liquid to flow downward in a stepped circular flow manner one by one, so that the back mixing phenomenon during liquid flow can be weakened, and the mass transfer driving force can be integrally improved. In addition, if a perforated tower plate provided with a specially-made bubbling element is adopted to replace a common sieve plate, gas tends to be condensed into larger gas masses in the bubbling element when rising, so that the gas flow is more stable and uniform, and the automatic operation elasticity adjusting capability along with the change of the gas flow is realized.
The stepped liquid circulation bubble tower provided by the invention improves the flow mode of continuous phase liquid, improves the operation stability of gas load change, and is expected to improve the integral effect of gas-liquid mass transfer. The detailed structure of the present invention will be described in detail in the summary of the invention and the detailed description.
Disclosure of Invention
The invention aims to provide a stepped liquid circulation bubble column and a method for dispersing gas, aiming at the defects of the prior art.
The purpose of the invention is realized by the following technical scheme: a stepped liquid circulation bubbling tower is composed of cylindrical tower wall, central partition plate, several horizontal semi-circular tower plates and L-shaped connecting tubes. The central partition plate penetrates through the whole tower from top to bottom, and divides the bubbling tower into a front bubbling area and a rear bubbling area; the semicircular tower plates are sequentially and alternately arranged at equal intervals from top to bottom in front of and behind the central partition plate, and the semicircular tower plate on the same side is positioned in the middle of two adjacent semicircular tower plates on the opposite side; the L-shaped communicating pipe connects the semicircular tower plates in front of and behind the central partition plate; the L-shaped communicating pipe is enclosed by a cylindrical tower wall, a central partition plate, two vertical side plates positioned in front of and behind the central partition plate and two horizontal bottom plates to form a front vertical channel and a rear vertical channel with different lengths; the top of two vertical channels of the L-shaped communicating pipe is open and is flush with the connected semicircular column plate respectively, the bottom of the two vertical channels is sealed by two front and rear bottom plates at the same height, and the two vertical channels are communicated by a circular opening of which the lower parts are positioned on the central partition plate.
Further, the length of the long channel of the front vertical channel and the length of the short channel of the rear vertical channel are 0.75 time of the distance between the tower plates on the same side of the central partition plate, and the length of the short channel of the front vertical channel and the rear vertical channel of the front vertical channel is 0.25 time of the distance between the tower plates on the same side of the central partition plate.
Further, the semicircular tower plate is a perforated plate provided with a plurality of bubbling elements.
Further, the distance between the tower plates of the semicircular tower plates on the same side is 150-300 mm.
Furthermore, the bubbling element is a conical baffle with an open top end and is provided with a conical bubbling panel, the lower end of the bubbling panel is fixed on the outer side of the annular sealing plate, and the lower end of the baffle is fixed on the inner side of the annular sealing plate.
Furthermore, the bubbling element is composed of an upper conical distribution cover and a lower conical gas-collecting cover which are concentric with the central axis; the upper conical distribution cover consists of a conical sieve plate with a sealed top end and a bottom annular sieve plate; the lower conical gas-collecting hood consists of a conical baffle with an open top end, a bottom annular blind plate and an inner two-stage defoaming screen plate; the inner two-stage defoaming screen plate consists of an upper cylindrical surface screen plate and a lower conical surface screen plate, and the middle parts of the upper cylindrical surface screen plate and the lower conical surface screen plate are connected by a round blind plate; the upper end of the cylindrical surface screen plate is connected with the upper end of the conical surface baffle plate, and the lower end of the conical surface screen plate is fixed on the inner side of the annular blind plate; the upper layer of conical distribution cover is sleeved outside the lower layer of conical gas-collecting hood and fixed to form a bubbling element; the bubbling element is fixed on the upper part of the semicircular column plate and is communicated with the opening of the semicircular column plate.
Furthermore, the bottom angles of the conical screen plates in the upper-layer conical distribution hood, the lower-layer conical gas-collecting hood and the gas-collecting hood are equal; the outer diameters of the bottom ends of the upper conical distribution cover and the lower conical gas collecting cover are equal; the size of the annular sieve plate at the bottom of the upper conical distribution cover is the same as that of the annular blind plate at the bottom of the lower conical gas-collecting cover.
Furthermore, the specification of sieve pores of the conical sieve plate and the bottom annular sieve plate is phi 2-4.5 mm, the sieve pores on the conical sieve plate are arranged according to a regular triangle or a square, the sieve pores on the annular sieve plate are arranged at equal intervals along two concentric circles, and the hole interval is 2.5-4.5 times of the hole diameter.
Furthermore, the inner two-stage defoaming screen plate is formed by the surrounding of punching screen plates, the meshes are rhombic, polygonal or cross-shaped, and the like, and the upper cylindrical surface screen plate and the lower conical surface screen plate can be the same screen plate or different screen plates.
A method for dispersing gas by using the stepped liquid circulation bubble column comprises the following steps:
before operation, the whole tower body is filled with process liquid.
The liquid is introduced from a liquid inlet at the highest position on the left side of the upper part of the tower body, transversely flows from left to right through a first semicircular tower plate behind the central partition plate, enters an L-shaped communicating pipe on the right side, flows downwards to the bottom of the communicating pipe, passes through the central partition plate, then flows upwards to a topmost tower plate in front of the partition plate, then transversely flows from right to left through the tower plates, enters the L-shaped communicating pipe on the left side, then flows to a second tower plate behind the central partition plate to complete a circulation passage, and finally is discharged from a bottom liquid outlet after the downward circulation flow plate; the gas enters from the bottom of the tower, is evenly divided into two parts by the gas distributor, enters the lower parts of the tower plates at the front side and the rear side of the central partition plate respectively, upwards passes through the bubbling element to be dispersed into the liquid above the tower plates, then is gathered and enters the lower part of the upper-stage tower plate, and finally flows upwards plate by plate and is discharged from a gas outlet at the top of the tower.
The invention has the beneficial effects that:
(1) the liquid can flow circularly downwards in a plate-by-plate stepped manner on two sides of the central partition plate, so that the liquid is favorable for weakening the back mixing phenomenon, and the mass transfer driving force can be integrally improved.
(2) The stepped liquid circulation bubbling tower provided by the invention takes liquid as a continuous phase and gas as a dispersed phase, and the gas forms an inclined upward opposite spraying phenomenon when passing through a specially-made bubbling element, so that the disturbance degree of gas-liquid contact is increased, and the mass transfer efficiency is improved.
(3) The special bubbling element of the stepped liquid circulation bubbling tower has the capability of adjusting the operation load, so that the elasticity is higher.
Drawings
FIG. 1 is a front and side view of a bubble column;
FIG. 2 is a schematic structural view of a two-end L-shaped communication pipe;
FIG. 3 is a schematic view showing the connection between the front and rear semicircular trays and the L-shaped communicating tube on one side;
FIG. 4 is a schematic view of two arrangements of sparging elements on a tray;
fig. 5 is a structural view of a first bubbling member;
fig. 6 is a structural view of a second bubbling member;
in the figure, a tower wall 1, a central partition plate 2, a semicircular tower plate 3, an L-shaped communicating pipe 4, a side plate 5, a bottom plate 6, a vertical channel 7, a circular opening 8, a bubbling element 9, a baffle 911, a bubbling panel 912, an annular closing plate 913, a conical distribution cover 921, a conical gas collection cover 922, a conical sieve plate 923, an annular sieve plate 924, a conical baffle 925, an annular blind plate 926, a cylindrical net plate 927, a conical net plate 928, a circular blind plate 929, a liquid inlet 10, a liquid outlet 11, a gas inlet 12, a gas distributor 13 and a gas outlet 14.
Detailed Description
The invention is described in further detail below with reference to the figures and the embodiments.
As shown in fig. 1-3, the present invention relates to a stepped liquid circulation bubble column, which is composed of a cylindrical column wall 1, a central partition plate 2, a plurality of horizontal semi-circular column plates 3 at equal intervals and an L-shaped communicating tube 4. The central partition plate 2 penetrates through the whole tower from top to bottom, and divides the bubbling tower into a front bubbling area and a rear bubbling area; the semicircular column plates 3 are sequentially and alternately arranged at equal intervals from top to bottom in front of and behind the central partition plate 2, and the semicircular column plate 3 on the same side is positioned in the middle of two adjacent semicircular column plates 3 on the opposite side; the L-shaped communicating pipe 4 connects the semicircular tower plates 3 at the front and the rear of the central partition plate 2; the L-shaped communicating pipe 4 is formed by enclosing a cylindrical tower wall 1, a central partition plate 2, two vertical side plates 5 (the vertical side plates 5 are vertically arranged with the central partition plate 2) positioned in front of and behind the central partition plate 2 and two horizontal bottom plates 6 to form a front vertical channel 7 and a rear vertical channel 7 with different lengths; the tops of two vertical channels 7 of the L-shaped communicating pipe 4 are open and are respectively flush with the connected semicircular tower plates 3, the bottoms of the two vertical channels are sealed by two front and rear bottom plates 6 at the same height, and the lower parts of the two vertical channels 7 are communicated with a circular opening 8 on the central partition plate 2.
Further, the length of the long channel of the front and rear vertical channels 7 is 0.75 time of the distance between the adjacent tower plates on the same side of the central partition plate 2, and the length of the short channel is 0.25 time of the distance between the adjacent tower plates on the same side of the central partition plate 2.
Further, the tower plate interval of the semicircular tower plates 3 on the same side of the stepped liquid circulation bubbling tower is 150-300 mm.
Further, the semicircular tray 3 of the stepped liquid circulation bubble column is a perforated plate equipped with a plurality of tailored bubbling elements 9, as shown in fig. 4.
Two examples of the bubbling element 9 are given below, but not limited thereto:
first bubbling element: as shown in fig. 5, the bubbling member 9 is a bubbling member having a tapered baffle 911 with an open top end and a tapered bubbling panel 912.
In some embodiments, the outer diameter of the bottom end of the bubbling element 9 is 50-120 mm; the lower end of the bubbling panel 912 is fixed on the outer side of the annular sealing plate 913, and the lower end of the baffle 911 is fixed on the inner side of the annular sealing plate 913; the bottom angles of the bubbling panel 912 and the baffle 911 are equal, and the size is 50-75 degrees; the height of the baffle 911 is 0.3-0.5 times of the height of the bubbling panel 912; the annular sealing plate 913 has an annular width of 0.12 to 0.2 times the outer diameter thereof.
The bubbling panel 912 is a conical screen plate with round holes of 2mm to 4.5mm in diameter, the round holes are arranged in regular triangle or square, and the hole pitch is 2.5 times to 4.5 times of the hole diameter.
Second bubbling element: as shown in fig. 6, the bubbling element 9 is composed of an upper conical distribution cover 921 and a lower conical gas-collecting cover 922 which are concentric with each other; the upper conical distribution cover 921 is composed of a conical screen plate 923 with a closed top end and a bottom annular screen plate 924; the lower-layer conical gas-collecting hood 922 consists of a conical baffle 925 with an open top end, a bottom annular blind plate 926 and an inner-layer two-stage defoaming screen plate; the inner two-stage defoaming screen plate consists of an upper cylindrical screen plate 927 and a lower conical screen plate 928, and the middle parts of the upper cylindrical screen plate and the lower conical screen plate are connected by a round blind plate 929; the upper end of the cylindrical screen plate 927 is connected with the upper end of the conical baffle 925, and the lower end of the conical screen plate 928 is fixed on the inner side of the annular blind plate 926; the upper layer of conical distribution cover 921 is sleeved outside the lower layer of conical gas-collecting cover 922 and fixed to form a bubbling element. The bubbling element is fixed on the upper part of the semicircular tower plate 3 and is communicated with the opening of the semicircular tower plate 3.
The gas gathers in the bubbling element 9 on the semicircular tower plate 3, passes through the conical screen plate 928 at the lower part upwards, enters between the two-stage defoaming plate and the conical baffle 925 of the conical gas collecting hood 922 at the lower layer, then passes through the cylindrical screen plate 927 upwards, enters the conical distribution hood 921 at the upper layer, continues to pass through the conical screen plate 923 at the upper layer of the conical distribution hood 921 upwards, and is dispersed into fine bubbles which enter the liquid outside the hood.
An annular gap channel is formed between the upper conical distribution cover 921 and the lower conical gas-collecting cover 922 of the bubbling element 9, so that a liquid phase is prevented from entering the distribution cover through the liquid seal effect when the gas phase flow is small, and the gas phase passes through the cover body quickly as a gas phase flow channel when the gas phase flow is large, thereby having the function of adjusting the operation elasticity.
Two stages of defoaming screen plates are arranged in the bubbling element 9, so that liquid beads with different sizes can be effectively removed, and the influence of liquid foam entrainment is favorably reduced.
In some embodiments, the bottom angles of the conical net plate 928 inside the upper conical distribution hood 921, the lower conical gas collection hood 922 and the gas collection hood are all equal and are 50-75 °.
The bottom external diameter of upper toper distribution cover 921 and lower floor toper gas collecting channel 922 is equal, and the size is 50 ~ 120 mm.
The height of the lower conical gas-collecting hood 922 is 0.5-0.75 times of that of the upper conical distribution hood 921.
The annular sieve plate 924 at the bottom of the upper conical distribution cover 921 is the same as the annular blind plate 926 at the bottom of the lower conical gas collection cover 922 in size, and the width of the ring is 0.12-0.2 times of the outer diameter of the bottom plate.
The sieve mesh specifications of the conical surface sieve plate 923 and the bottom annular sieve plate 924 of the upper conical distribution cover 921 are phi 2-4.5 mm, the sieve meshes on the conical surface sieve plate 923 are arranged according to a regular triangle or a square, the sieve meshes on the annular sieve plate 924 are arranged along two concentric circles at equal intervals, and the hole interval is 2.5-4.5 times of the hole diameter.
The inner two-stage defoaming screen plate is formed by surrounding punching screen plates, the meshes are rhombic, polygonal or cross-shaped, and the like, and the upper cylindrical surface screen plate 927 and the lower conical surface screen plate 928 can be the same screen plate or different screen plates.
The invention also provides a method for dispersing gas by using the stepped liquid circulation bubble column, which comprises the following steps:
before operation, the whole tower body is filled with process liquid.
The liquid is introduced from a liquid inlet 10 at the highest position on the left side of the upper part of the tower body, transversely flows through a first semicircular tower plate 3 behind a central partition plate 2 from left to right to enter an L-shaped communicating pipe 4 on the right side, flows downwards to the bottom of the communicating pipe, passes through the central partition plate 2, then flows upwards to a topmost tower plate 3 in front of the partition plate, then transversely flows through the tower plates from right to left to enter the L-shaped communicating pipe 4 on the left side, then flows to a second tower plate behind the central partition plate 2 to complete a circulation path, and finally is discharged from a bottom liquid outlet 11 after the downward circulation flow; the gas enters from a gas inlet 12 at the bottom of the tower, is evenly divided into two parts by a gas distributor 13, enters the lower parts of the tower plates at the front side and the rear side of the central partition plate 2 respectively, passes through the bubbling element 9 upwards to be dispersed into the liquid above the tower plates, is gathered and enters the lower part of the upper-stage tower plate, flows upwards plate by plate in the way, and is finally discharged from a gas outlet 14 at the top of the tower.
The structure of the present invention will be further described with reference to specific examples, but the present invention should not be construed as being limited thereto.
Example 1
FIG. 1 represents a schematic view of a stepped liquid circulation bubble column having a diameter of 250mm, wherein semicircular trays 8 are provided on both sides of a central partition plate, the spacing between the trays on the same side is 160mm, and 2 first type of conical bubbling elements are disposed on each semicircular tray (FIG. 4 a).
The L-shaped communicating pipe structure is shown in figure 2, the height of the vertical channel is 120mm and 40mm respectively, and the width of the side plate is 85 mm.
The structure of the bubbling element is shown in fig. 5, the bottom angle of the conical bubbling panel is 63.5 degrees, the outer diameter and the height of the bottom end are both 60mm, the height of the internal conical baffle is 22mm, the bottom angle is also 63.5 degrees, and the width of the annular closing plate is 9 mm. 164 round holes with the diameter of 2mm are arranged on the conical bubbling panel in a regular triangle, and the distance between the holes is 6 mm.
The air is humidified by adopting the stepped liquid circulation bubbling tower, the air at 25 ℃ enters from a gas inlet at the bottom of the tower, and the total flow rate is 120Nm3H, humidity of 0.0075kg/kg dry air; 50 ℃ water enters from a liquid inlet at the top of the tower, and the flow rate is 0.5m3H is used as the reference value. The wet air temperature at the outlet of the overhead gas was measured to be 42 ℃ and the humidity was 0.0472kg/kg of dry air.
Example 2
The bubble column structure was the same as in example 1.
Air at 25 ℃ was introduced from the bottom gas inlet with a total flow of 95Nm3H, humidity of 0.0075kg/kg dry air; 50 ℃ water enters from a liquid inlet at the top of the tower, and the flow rate is 0.4m3H is used as the reference value. The wet air temperature at the top gas outlet was measured to be 44 ℃ and the humidity was measured to be 0.0507kg/kg dry air.
Example 3
The bubble column structure was the same as in example 1.
Air at 25 ℃ is introduced from the bottom gas inlet with a total flow of 100Nm3H, humidity of 0.0075kg/kg dry air; 50 ℃ aqueous solution containing 20 wt.% calcium chloride enters from the top liquid inlet at a flow rate of 0.5m3H is used as the reference value. The temperature of the wet air at the outlet of the overhead gas was measured to be 43 ℃ and the humidity was 0.0484kg/kg of dry air.
Example 4
FIG. 1 shows a schematic diagram of a stepwise liquid circulation bubble column having a diameter of 600mm, 16 semicircular trays respectively provided on both sides of a central partition plate, the spacing between the trays on the same side being 200mm, and 12 second type of conical bubbling elements arranged in regular triangles on each semicircular tray (FIG. 4 b).
The L-shaped communicating pipe structure is shown in figure 2, the height of the vertical channel is 150mm and 50mm respectively, and the width of the side plate is 200 mm.
The structure of the bubbling element is shown in fig. 6, the bottom angle of the conical cover is 63.5 degrees, the outer diameter of the bottom end is 60mm, and the height of the upper conical distribution cover is 60 mm; the height of the lower conical gas-collecting hood is 40 mm; the size of the annular sieve plate at the bottom of the upper conical distribution cover is the same as that of the annular blind plate at the bottom of the lower conical gas-collecting cover, and the width of the annular sieve plate is 10 mm; the specification of the round holes of the conical screen plate of the upper conical distribution cover and the bottom annular screen plate is phi 2mm, the number of the round holes on the conical screen plate is 164, the round holes are arranged according to a regular triangle (the same as that in the figure 5, the hole spacing is 6mm), the sieve holes on the annular screen plate are arranged at equal intervals along two concentric circles, and the diameters of the concentric circles are 45mm and 55mm respectively (22 and 28 equidistant round holes respectively).
The stepwise liquid circulation bubble column is used for absorbing acetone gas in air, and air and acetone mixed gas (acetone volume fraction of 0.083) at 25 ℃ enters from a gas inlet at the bottom of the column, and the total flow rate is 500Nm3H, water at 25 ℃ enters from a liquid inlet at the top of the tower, and the flow rate is 1.8m3H is used as the reference value. The acetone absorption after stabilization was 90.8%.
Example 5
The bubble column structure was the same as in example 4.
When the flow rate of the air-acetone mixed gas (acetone volume fraction 0.083) at 25 ℃ is 650Nm3At a flow rate of 2.4m at 25 ℃3At the time of/h, the absorption of acetone after stable operation was 88.6%.
Example 6
The bubble column structure was the same as in example 4.
When the flow rate of the air-acetone mixed gas (acetone volume fraction 0.083) at 25 ℃ is 500Nm3At a flow rate of 2.4m at 25 ℃3At/h, the absorption of acetone after steady operation was 96.9%.
The above-described embodiments are intended to illustrate rather than to limit the invention, and any modifications and variations of the present invention are within the spirit of the invention and the scope of the appended claims.
Claims (6)
1. A stepped liquid circulation bubbling tower is characterized in that the bubbling tower is composed of a cylindrical tower wall, a central partition plate, a plurality of horizontal semi-circular tower plates with equal intervals and an L-shaped communicating pipe; the central partition plate penetrates through the whole tower from top to bottom, and divides the bubbling tower into a front bubbling area and a rear bubbling area; the semicircular tower plates are sequentially and alternately arranged at equal intervals from top to bottom in front of and behind the central partition plate, and the semicircular tower plate on the same side is positioned in the middle of two adjacent semicircular tower plates on the opposite side; the L-shaped communicating pipe connects the semicircular tower plates in front of and behind the central partition plate; the L-shaped communicating pipe is enclosed by a cylindrical tower wall, a central partition plate, two vertical side plates positioned in front of and behind the central partition plate and two horizontal bottom plates to form a front vertical channel and a rear vertical channel with different lengths; the top parts of two vertical channels of the L-shaped communicating pipe are open and are respectively flush with the connected semicircular tower plates, the bottom parts of the two vertical channels are sealed by two front and rear bottom plates at the same height, and the lower parts of the two vertical channels are communicated with a circular opening on the central partition plate;
the semicircular tower plate is a porous plate provided with a plurality of bubbling elements; the bubbling element consists of an upper conical distribution cover and a lower conical gas-collecting cover which are concentric with the central shaft; the upper conical distribution cover consists of a conical sieve plate with a sealed top end and a bottom annular sieve plate; the lower conical gas-collecting hood consists of a conical baffle with an open top end, a bottom annular blind plate and an inner two-stage defoaming screen plate; the inner two-stage defoaming screen plate consists of an upper cylindrical surface screen plate and a lower conical surface screen plate, and the middle parts of the upper cylindrical surface screen plate and the lower conical surface screen plate are connected by a round blind plate; the upper end of the cylindrical surface screen plate is connected with the upper end of the conical surface baffle plate, and the lower end of the conical surface screen plate is fixed on the inner side of the annular blind plate; the bottom angles of the conical screen plates in the upper conical distribution cover, the lower conical gas collecting cover and the gas collecting cover are equal; the outer diameters of the bottom ends of the upper conical distribution cover and the lower conical gas collecting cover are equal; the size of the annular sieve plate at the bottom of the upper conical distribution hood is the same as that of the annular blind plate at the bottom of the lower conical gas collecting hood;
the upper-layer conical distribution cover of the bubbling element is sleeved outside the lower-layer conical gas-collecting hood and fixed, and the bubbling element is fixed on the upper part of the semicircular column plate and communicated with the opening of the semicircular column plate when in use.
2. The stepped liquid circulation bubble column according to claim 1, wherein the length of the long passage of said front and rear vertical passages is 0.75 times the distance between the trays on the same side of the central partition plate, and the length of the short passage is 0.25 times the distance between the trays on the same side of the central partition plate.
3. The stepped liquid circulation bubble column according to claim 1, wherein the tray pitch of the semicircular trays on the same side is 150 to 300 mm.
4. The cascade liquid circulating bubble column as claimed in claim 1, wherein the mesh size of the conical screen plate and the bottom annular screen plate is 2 to 4.5mm, the mesh size of the conical screen plate is regular triangle or square, the mesh size of the annular screen plate is equal to the mesh size of the conical screen plate, and the mesh size of the annular screen plate is 2.5 to 4.5 times the diameter of the holes.
5. A stepped liquid circulating bubble column as claimed in claim 1, wherein the inner two-stage defoaming screens are formed by punching screens, the meshes are polygonal or cross-shaped, and the upper cylindrical screen and the lower conical screen may be the same screen or different screens.
6. A method of dispersing gas using a stepped liquid loop bubble column according to any one of claims 1 to 5, comprising the steps of:
filling the whole tower body with process liquid before operation;
the liquid is introduced from a liquid inlet at the highest position on the left side of the upper part of the tower body, transversely flows from left to right through a first semicircular tower plate behind the central partition plate, enters an L-shaped communicating pipe on the right side, flows downwards to the bottom of the communicating pipe, passes through the central partition plate, then flows upwards to a topmost tower plate in front of the partition plate, then transversely flows from right to left through the tower plates, enters the L-shaped communicating pipe on the left side, then flows to a second tower plate behind the central partition plate to complete a circulation passage, and finally is discharged from a bottom liquid outlet after the downward circulation flow plate; the gas enters from the bottom of the tower, is evenly divided into two parts by the gas distributor, enters the lower parts of the tower plates at the front side and the rear side of the central partition plate respectively, upwards passes through the bubbling element to be dispersed into the liquid above the tower plates, then is gathered and enters the lower part of the upper-stage tower plate, and finally flows upwards plate by plate and is discharged from a gas outlet at the top of the tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911302733.XA CN111013178B (en) | 2019-12-17 | 2019-12-17 | Stepped liquid circulation bubble tower and method for dispersing gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911302733.XA CN111013178B (en) | 2019-12-17 | 2019-12-17 | Stepped liquid circulation bubble tower and method for dispersing gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111013178A CN111013178A (en) | 2020-04-17 |
| CN111013178B true CN111013178B (en) | 2021-06-22 |
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| CN108245929B (en) * | 2018-01-15 | 2019-06-14 | 浙江大学 | A kind of method of interlayer cone cover dispersive element and dispersion phase |
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