CN110354523B - Novel column plate with microporous bubble cap - Google Patents
Novel column plate with microporous bubble cap Download PDFInfo
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- CN110354523B CN110354523B CN201910632863.3A CN201910632863A CN110354523B CN 110354523 B CN110354523 B CN 110354523B CN 201910632863 A CN201910632863 A CN 201910632863A CN 110354523 B CN110354523 B CN 110354523B
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- 239000007788 liquid Substances 0.000 claims abstract description 81
- 238000007664 blowing Methods 0.000 claims abstract description 5
- 238000012546 transfer Methods 0.000 abstract description 17
- 238000010521 absorption reaction Methods 0.000 abstract description 12
- 230000005587 bubbling Effects 0.000 abstract description 5
- 230000001737 promoting effect Effects 0.000 abstract description 2
- 238000010977 unit operation Methods 0.000 abstract description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 8
- 238000002156 mixing Methods 0.000 description 6
- 238000002347 injection Methods 0.000 description 5
- 239000007924 injection Substances 0.000 description 5
- 238000012360 testing method Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007667 floating Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000006096 absorbing agent Substances 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 1
- 238000009954 braiding Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000010668 complexation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000005501 phase interface Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
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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
- B01D3/18—Fractionating columns in which vapour bubbles through liquid with horizontal bubble plates
-
- 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
- B01D3/18—Fractionating columns in which vapour bubbles through liquid with horizontal bubble plates
- B01D3/20—Bubble caps; Risers for vapour; Discharge pipes for liquid
- B01D3/205—Bubble caps
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The invention discloses a novel column plate with microporous bubble caps, which comprises a column plate, wherein a plurality of microporous bubble caps for finely dividing gas into microbubbles and blowing the microbubbles at an angle with the horizontal direction are arranged on the column plate at intervals, each microporous bubble cap comprises a plurality of full-mesh bubble caps which are arranged in the central area of the column plate and are arranged at the liquid inlet end and higher than the overflow weir end, and a plurality of half-mesh bubble caps which are arranged in the arch area of the column plate and are respectively formed with corners with the central line of the overflow weir. The invention has the characteristics of reducing the liquid level gradient, reducing the non-activated area, enabling the liquid to flow uniformly and stably, increasing the contact area of the gas and the liquid, promoting the bubbling of the liquid, increasing the disturbance of the air flow to the liquid when passing through the liquid layer and improving the contact efficiency of the gas and the liquid, is suitable for gas-liquid and liquid-liquid contact mass transfer equipment, and completes the unit operations of absorption, rectification, heat exchange and the like.
Description
Technical Field
The invention belongs to the technical field of gas-liquid and liquid-liquid contact mass transfer equipment, and particularly relates to a novel column plate with a microporous bubble cap.
Background
The tower is a gas-liquid and liquid-liquid contact mass transfer device widely applied in petroleum, chemical industry, light industry and medicine industry, and completes unit operations such as absorption, rectification, heat exchange and the like. Trays are among the most basic, important components, determining the performance of the column. The structure can be divided into bubble cap tray, sieve pore tray, float valve tray, tongue tray, etc.
(1) The bubble cap tray is the tray used in the earliest industry and mainly consists of a riser and bubble caps. The bubble cap is arranged at the top of the riser, is round, and has a plurality of tooth gaps at the periphery of the lower part. The structure is complex, the pressure drop is large, bubbles are difficult to contact with liquid at the lower end area of the tooth gap, backmixing exists, insufficient gas-liquid contact is caused, and the tray efficiency is greatly influenced. (2) The sieve trays have a plurality of small holes, shaped as sieves, and are provided with or without overflow tubes. The operation elasticity is small, and when the air speed is low, the liquid leakage is serious. (3) The valve plate is based on bubble cap plate and sieve mesh plate, and has several kinds of valve, but has similar basic structure, i.e. holes are formed in the plate in certain arrangement, valve plates capable of floating upwards and downwards in the axial direction are set over the holes, and the valve plates may be regulated automatically with the change of the rising air amount. The valve plate is easy to be blocked, and free opening of the valve plate is affected. (4) The tongue-shaped column plate is an oblique jet column plate, a plurality of tongue-shaped holes are punched on the column plate according to a certain arrangement, and the upward opening angle of the tongue piece is about 20 degrees. The opening angle is fixed, when the air quantity is smaller, the air speed sprayed through the tongue hole is low, the liquid leakage of the tower plate is serious, and the operation elasticity is small.
The guide sieve plate starts from the gas-liquid momentum balance of different areas of the tower plate, and the distribution and the rotation angle of the guide holes are arranged according to the principle that the gas sprayed from the guide holes pushes the liquid to advance, and the momentum transferred to the liquid is equal to the momentum required by the liquid to overcome the advancing resistance. The liquid layer in the upstream region is reduced in thickness, and the trace of the liquid flow is changed to induce and promote bubbling of the liquid. In addition, in the upstream region of the liquid flow, the liquid releases the contained gas during the flowing down from the downcomer, so the liquid just entering the upstream region is a real liquid and is difficult to bubble by the ascending gas (the gas and the liquid are subjected to mass transfer on the bubbling surface), thus forming a 'non-activated zone' on the tray, generally about 30%, and greatly affecting the tray efficiency and the production capacity.
CN1298751a discloses a column plate, which is a double-layer column plate formed by arranging a layer of additional mass transfer components, such as a sieve plate, an apertured plate, a net plate, a silk screen braiding plate, etc., on a conventional column plate. The aperture ratio or the porosity of the additional column plate is higher than that of the lower column plate, and by adopting the column plate, the upper space of the column plate can be fully utilized, a larger phase interface area and longer residence time are provided for the gas-liquid two phases, and the mass transfer efficiency of the column plate is improved. However, the tray requires a larger flow rate of liquid phase, the liquid phase can play the role of the accessory part only after passing through the accessory mass transfer part, and the problem of insufficient contact between the lower interface and the liquid and back mixing still exists. CN2604219Y discloses a combined porous medium bubble-cap column plate, which combines two heat and mass transfer modes of injection and bubbling, a horizontal column plate with air lifting holes is arranged in the column, a liquid lifting ring is arranged above each air lifting hole, an injection cover is arranged on the outer side of the liquid lifting ring, the injection cover is not provided with holes, a baffle is not arranged at the top end of the injection cover, and a bottom gap is arranged between the injection cover and the column plate. A section of porous medium or filler is filled between the outermost cover body and the jet cover, and the outer cover body is provided with uniform exhaust holes at the part below the filling layer. However, there is baffling, there is back mixing, and the column plate structure is complex, and installation, maintenance are difficult. CN100388959C discloses a porous surface column plate, its surface has a porous layer, the porosity of the porous layer is 15% -45%, average pore diameter is 10-200 micrometers, average thickness is 0.2-0.8 mm. Because the surface of the tower plate is provided with a porous layer, under the condition that the temperature difference (0.2-1 ℃) between the upper side and the lower side of the tower plate is small, components with relatively high volatility in the liquid phase on the surface of the tower plate are vaporized and separated, and the tower plate is mainly used for improving the rectification operation tower plate and is ineffective for the absorption operation.
Disclosure of Invention
The invention provides a novel column plate with microporous bubble caps, which is used for reducing the liquid level gradient, reducing a non-activated zone, enabling liquid to flow uniformly and stably, increasing the contact area of gas and liquid, promoting bubbling of the liquid, increasing disturbance of the gas flow to the liquid when the gas flow passes through a liquid layer, and improving the gas-liquid contact efficiency.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
the novel column plate comprises a column plate, wherein a plurality of microporous gas bubble caps for finely dividing gas into microbubbles and blowing out the microbubbles at an angle with the horizontal direction are arranged on the column plate at intervals, each microporous gas bubble cap comprises a plurality of full-mesh gas bubble caps which are arranged in the central area of the column plate and at the liquid inlet end and higher than the overflow weir end, and a plurality of half-mesh gas bubble caps which are arranged in the arch area of the column plate and are respectively provided with corners with the central line of the overflow weir.
Further, the full-mesh bubble cover comprises a round table-shaped micropore distribution full mesh constructed between the first supporting round table and the first upper round table, the small diameter end and the large diameter end of the micropore distribution full mesh are respectively connected with the first supporting round table and the first upper round table, the axes of the small diameter end and the large diameter end are overlapped, a first connecting sleeve extends on the first supporting round table along the axis of the first connecting sleeve in the direction away from the first upper round table, and the first connecting sleeve is detachably connected with the tower plate.
Further, the aperture of the micropore distribution whole net is 10-300 mu m, the diameter ranges of the first supporting round table and the first upper round table are 10-100 mm, the ratio of the height of the whole net type bubble cover to the height of the first supporting round table is 0.5-4, and the angle between the inclined edge of the micropore distribution whole net and the end face of the first supporting round table is 0-180 degrees.
Further, the half-mesh bubble cap comprises a truncated cone-shaped micropore distribution half-mesh constructed between the second support truncated cone and the second upper truncated cone, the small-diameter end and the large-diameter end of the micropore distribution half-mesh are respectively connected with the second support truncated cone and the second upper truncated cone, the axes of the small-diameter end and the large-diameter end are coincident with each other, a second connecting sleeve extends on the second support truncated cone along the axis of the second support truncated cone in the direction away from the second upper truncated cone, and the second connecting sleeve is detachably connected with the tower plate.
Further, the aperture of the micropore distribution half-net is 10-300 mu m, the diameter ranges of the second supporting round table and the second upper round table are both 10-100 mm, the ratio of the height of the half-net type bubble cover to the height of the second supporting round table is 0.5-4, and the angle between the bevel edge of the micropore distribution half-net and the end face of the second supporting round table is 0-180 degrees.
Further, the whole-net type air bubble cap arranged at the liquid inlet end of the tower plate is 0.5-5 mm higher than the whole-net type air bubble cap arranged at the overflow weir end.
Further, the full-mesh type air bubble caps are arranged in a regular triangle, and the distance between every two adjacent full-mesh type air bubble caps is 60mm.
Further, the included angles between the central lines of the half-mesh type air bubble caps and the central line of the overflow weir are 38 degrees, 48 degrees and 62 degrees respectively.
Furthermore, the novel tower plates with the microporous bubble caps are arranged at intervals along the flow direction of the gas in the tower body, and the distance between the adjacent tower plates is 200-300mm.
Compared with the prior art, the invention adopts the structure, and the technical progress is that: when gas passes through the tower plate, the gas is blown out through micropores of the microporous bubble cap to form micro bubbles, and the gas-liquid mass transfer rate is inversely proportional to the diameter of the bubbles, so that the gas-liquid contact time and the contact area are increased by the micro bubbles, the gas-liquid mass transfer efficiency is improved, and meanwhile, the flux of the gas is improved by the microporous bubble cap, and the operation flexibility is improved; the flow conditions of each point in the arched area of the tower plate are different, the side surface of the half-mesh bubble cap is adopted for blowing out, and the symmetrical center line of the half-mesh bubble cap and the center line direction of the overflow weir of the tower plate have certain corners, so that the liquid flow distribution in different areas on the tower plate is uniform and stable; from the gas-liquid momentum balance calculation of different areas of the tower plate, the distribution of the microporous gas bubble caps and the inclination angle of the side face are arranged according to the principle that the gas sprayed from the microporous gas bubble caps pushes the liquid to advance, and the momentum transferred to the liquid is equal to the momentum required by the liquid to overcome the advancing resistance, so that the invention has the characteristics of uniformity of gas-liquid contact and reduction of back mixing.
Drawings
The accompanying drawings are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate the invention and together with the embodiments of the invention, serve to explain the invention.
In the drawings:
FIG. 1 is a schematic diagram showing the distribution of microporous bubble hoods on a tray according to an embodiment of the present invention;
FIG. 2 is a schematic view of the structure of a full mesh type bubble cap according to an embodiment of the present invention;
fig. 3 is a schematic structural view of a half-mesh type bubble cap according to an embodiment of the present invention.
Marking parts: 1-micropore distribution half net, 2-second support round platform, 3-second upper round platform, 4-second connecting sleeve, 5-lock nut, 6-micropore distribution full net, 7-first support round platform, 8-first upper round platform, 9-first connecting sleeve, 10-column plate and 11-mounting hole.
Detailed Description
Preferred embodiments of the present invention will be described below with reference to the accompanying drawings. It should be understood that the preferred embodiments described herein are presented for purposes of illustration and explanation only and are not intended to limit the present invention.
Example novel tray with microporous bubble cap
The embodiment discloses a novel column plate with microporous bubble caps, as shown in fig. 1-3, the novel column plate comprises a column plate 10 and a plurality of microporous bubble caps, a plurality of mounting holes 11 are formed in the column plate 10, each microporous bubble cap is detachably mounted on the column plate 10 through the corresponding mounting hole 11, and the microporous bubble caps are used for refining gas into microbubbles and blowing out the microbubbles at an angle with the horizontal direction. The side micropores of the microporous bubble cap and the horizontal square form an angle a, the angle a is 0-90 degrees, bubbles with the same size as meshes are formed, the liquid disturbance is increased, the contact time is prolonged, the smaller the meshes are, the smaller the microbubbles are, the larger the gas-liquid contact area is, and the heat transfer and mass transfer efficiency is higher. Wherein the microporous gas bubble cap comprises a plurality of full-mesh gas bubble caps and a plurality of half-mesh gas bubble caps, the full-mesh gas bubble caps are arranged in the central area of the tray 10, and the full-mesh gas bubble caps arranged at the liquid inlet end are 0.5-5 mm, preferably 1-2 mm, higher than the full-mesh gas bubble caps arranged at the overflow weir end, so that the 'non-activated zone' is effectively reduced, the thickness of an upstream liquid layer is reduced, and the liquid level gradient is reduced; these half-mesh bubble caps are mounted in the arcuate region of tray 10 and form corners with the weir centerlines, respectively.
The full-mesh bubble cap of the invention has a preferable structure as shown in fig. 2, and comprises a first supporting circular table 7, a first upper circular table 8 and a micropore distribution full-mesh 6, wherein the micropore distribution full-mesh 6 is in a circular table-shaped structure, is fixedly arranged between the first supporting circular table 7 and the first upper circular table 8, the small diameter end and the large diameter end of the micropore distribution full-mesh 6 are respectively connected with the first supporting circular table 7 and the first upper circular table 8, the axes of the small diameter end and the large diameter end are overlapped, a first connecting sleeve 9 extends on the first supporting circular table 7 along the axis of the first supporting circular table 7 in a direction far away from the first upper circular table 8, and the first connecting sleeve 9 is inserted into a mounting hole 11 positioned in the central area of a column plate 10 and is fastened on the column plate 10 through a locking nut 5 in threaded connection with the first connecting sleeve 9.
The half-mesh bubble cap of the invention has a preferable structure, as shown in fig. 3, and comprises a second supporting circular table 2, a second upper circular table 3 and a micropore distribution half-mesh 1, wherein the micropore distribution half-mesh 1 is in a circular table-shaped structure, and is fixedly arranged between the second supporting circular table 2 and the second upper circular table 3, the small diameter end and the large diameter end of the micropore distribution half-mesh 1 are respectively connected with the second supporting circular table 2 and the second upper circular table 3, the axes of the small diameter end and the large diameter end are overlapped, a second connecting sleeve 4 extends on the second supporting circular table 2 along the axis of the second supporting circular table 2 in a direction far away from the second upper circular table 3, and the second connecting sleeve 4 is inserted into a mounting hole 11 positioned in an arch region of a tray 10 and is fastened on the tray 10 through a locking nut 5 in threaded connection with the second connecting sleeve 4.
In order to facilitate manufacturing, installation, replacement and maintenance, the full-mesh type bubble cap and the half-mesh type bubble cap have similar structures, and the difference is that one adopts a micropore distribution full-mesh 6, the other adopts a micropore distribution half-mesh 1, the micropore distribution half-mesh 1 means that the side surface is provided with about half of meshes, and the rest side surface is in a closed state. The pore diameters of the microporous distribution full net 6 and the microporous distribution half net 1 are 10-300 mu m, preferably 80-150 mu m. The diameter ranges of the first supporting round table 7, the first upper round table 8, the second supporting round table 2 and the second upper round table 3 are all 10-100 mm, and the preferred diameter ranges of the first supporting round table 7 and the second supporting round table 2 are all 20-50 mm. The ratio of the height of the full-mesh type air bubble cap to the first supporting round table 7 and the ratio of the height of the half-mesh type air bubble cap to the second supporting round table 2 are both 0.5-4, the preferable ratio is 1.5-3, the angle of the inclined edge of the micropore distribution full-mesh 6 to the end face of the first supporting round table 7 and the angle of the inclined edge of the micropore distribution half-mesh 1 to the end face of the second supporting round table 2 are both 0-180 degrees, and the preferable angle is 45-90 degrees. According to the invention, the thicknesses of the first supporting round table 7 and the second supporting round table 2 are as small as possible, so that gaps between the tower plates 10 and the microporous bubble covers are as small as possible, and the uniformity of gas-liquid mixing is improved. The gas resistance is determined by the size of micropores and the height of the liquid level, and when the gas passes through the side surface with larger area, the aperture ratio is generally 30-40%; if the microporous air bubble cap with the aperture of 150 mu m of the microporous distribution full net 6 and/or the microporous distribution half net 1 is selected, the resistance is mainly determined by the liquid level; if the microporous air bubble cap with the pore diameter of 50 μm of the microporous distribution full net 6 and/or the microporous distribution half net 1 is selected, the resistance is mainly determined by micropores. Aiming at the situation that the smaller the micropores are, the larger the resistance is, and a fan with higher pressure can be adopted in the absorption process, so that gas passes through the microporous bubble cap, and the aim of uniformly mixing gas and liquid is fulfilled; aiming at the problem that micropores are smaller and easier to block, the process finds that the first supporting round table 7 is smaller than the first upper round table 8, and the second supporting round table 2 is smaller than the second upper round table for 3 hours, so that the micropores are difficult to block; this is due to the fact that in the process, the sealing sheets of the first upper circular table 8 or the second upper circular table 3 are large, which is equivalent to a cap, so that impurities are not easy to fall on the side microporous net.
The invention adopts microporous bubbles with the tower diameter of 400mmThe pilot tower is capped to absorb acetone from the configuration gas and one of a variety of tests is performed to illustrate this. The material of the micro-bubble cover test tower is stainless steel, and the gas flow rate is 400m when the gas flow rate is high 3 /h, low time 80m 3 And/h, the flow rate of the liquid absorbent is 300L/h; the structure of a plurality of the present examples is adopted, and the novel trays with microporous bubble caps are arranged at intervals along the flow direction of the gas in the column body for absorption, and the interval between the adjacent trays 10 is 200-300mm, preferably 250mm. The number of novel trays of the microporous bubble cap is four as an example, the arrangement mode is shown in figure 1, the central area of the tray 10 is arranged in a regular triangle, the aperture of the mounting holes 11 is 21mm or 22mm, and the distance between the adjacent mounting holes 11 is 60mm; the angles of the center line of the half-mesh air bubble cap and the center line of the overflow weir in the arcuate region are 38 °, 48 °, 62 ° respectively as identified in fig. 1.
As shown in fig. 2 and 3, the full-mesh type bubble cap and the half-mesh type bubble cap are provided with a micropore distribution full-mesh 6 and a micropore distribution half-mesh 1, the aperture of the mesh is 150 μm, the aperture ratio is 33%, the diameters of the first supporting round table 7 and the second supporting round table 2 are 20mm, and the diameters of the first upper round table 8 and the second upper round table 3 are 40mm; the length of the oblique sides of the micropore distribution full mesh 6 and the micropore distribution half mesh 1 is 40mm, and the angles of the oblique sides of the micropore distribution full mesh 6 and the micropore distribution half mesh 1 and the corresponding first supporting round table 7 and second supporting round table 2 are 75 degrees. The threads of the first connecting sleeve 9 or the second connecting sleeve 4 which are connected with the column plate 10 of the microporous bubble cap are M20X1.5.
An overflow weir is arranged in the tower, and the height of the overflow weir is 40mm; the following gas-liquid absorption operation conditions are as follows,
(1) Air inflow 400m 3 /h, acetone gas concentration 20000mg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The spraying amount of the top absorbent is 300L/h, and the circulating spraying amount of the middle absorbent is 3000L/h. The gas passes through the microporous bubble cap, the liquid flows in from the upper stage tray 10, the gas forms dense and tiny bubbles which are blown out at an angle of about 15 degrees with the horizontal direction, and the bubbles contact with the liquid for mass transfer to form a foam state; the resistance of the tower plate 10 is about 500Pa, and the detected outlet gas concentration reaches 500mg/m 3 The organic gas removal rate was about 97.5%.
(2) Air intakeWith a quantity of 80m 3 And/h, the concentration of acetone gas in the inlet gas is 10000mg/m 3 Resistance about 400Pa, liquid in the tower not leaking due to gas quantity reduction, and detected gas outlet concentration about 400/m 3 The organic gas removal rate was 96%.
The microporous bubble cap test tower and the floating valve tower with the same tower plate number of 10 were compared under the same operation condition, and the results are shown in the following table 1:
TABLE 1 comparison of the effects of a microporous bubble cap test tower absorber with a float valve absorber under the same operating conditions
As can be seen from table 1, the effect of absorbing acetone gas by using the microporous bubble cap test tower is better than that by using the floating valve tray 10 under the same air inflow and the same inlet gas concentration; it can be seen that the novel tray 10 composed of microporous bubble caps has good effect on VOC gas absorption.
The invention has the following main advantages:
(1) The gas passes through the side surface of the bubble cover with larger area, so that the gas speed is reduced, the gas-liquid contact time is prolonged, and the gas flux is larger; (2) Micro-scale bubbles are formed through the microporous bubble cap, so that the gas-liquid contact area is increased, and the gas-liquid contact is more uniform; (3) The gas bubble caps with different heights are arranged in different areas, and the half-net type gas bubble caps with different angles with the central line of the overflow weir are arranged in the arched areas, so that the gradient of the liquid level is reduced, and the uniform mixing of gas and liquid is facilitated; and (4) the microporous bubble cover is convenient to install, overhaul and replace.
According to the requirements of stable and uniform flow of liquid flow in different areas of the tower plate 10, the air bubble caps are reasonably arranged, the air bubble caps with different heights and the half-mesh air bubble caps with different angles in the arched areas are adopted in the area of the tower plate 10, and the non-activated area (which can be reduced from 30% to about 5%) on the tower plate 10 is basically eliminated. And the micropore direction of the micropore bubble cover side forms a certain angle with the horizontal direction, so that the number of bubbles on the tower plate 10 and the gas-liquid contact area are increased, certain disturbance is caused to liquid, and the plate efficiency is greatly improved. The absorption mass transfer efficiency of the tower plate 10 of the invention is about 70-95% through experiments.
The invention can be used for gas-liquid mass transfer equipment in chemical process, and is characterized in that microporous gas bubble caps are arranged on the tower plate 10, fine and uniform bubbles are obtained by utilizing the microporous gas bubble caps, the gas-liquid dispersion condition in the gas-liquid contact equipment is improved, and the gas-liquid mass transfer capability is enhanced, so that higher mass transfer capability is achieved under lower energy consumption, and the invention can be used for absorption and distillation operation, especially can be used for gas absorption with larger fluctuation range of gas quantity, and can be used for improving the concentration of absorption liquid and reducing the absorption operation cost.
Finally, it should be noted that: the foregoing description is only a preferred embodiment of the present invention, and the present invention is not limited thereto, but it is to be understood that modifications and equivalents of some of the technical features described in the foregoing embodiments may be made by those skilled in the art, although the present invention has been described in detail with reference to the foregoing embodiments. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the scope of the claims of the present invention.
Claims (9)
1. A novel tray with microporous bubble cap, includes tray, its characterized in that: a plurality of microporous air bubble caps for finely dividing air into microbubbles and blowing out the microbubbles at an angle with the horizontal direction are arranged on the tower plate at intervals, each microporous air bubble cap comprises a plurality of full-mesh-type air bubble covers which are arranged in the central area of the tower plate and are arranged at the liquid inlet end and higher than the overflow weir end, and each full-mesh-type air bubble cover comprises a truncated cone-shaped microporous distribution full mesh which is constructed between a first supporting truncated cone and a first upper truncated cone; and a plurality of half-mesh bubble covers which are arranged in the arch area of the column plate and form included angles with the central line of the overflow weir respectively, wherein the half-mesh bubble covers comprise truncated cone-shaped micropore distribution half-meshes which are constructed between the second supporting truncated cone and the second upper truncated cone, the micropore distribution half-meshes are meshes of about half of the side surfaces, and the rest side surfaces are in a closed state.
2. A novel tray with microporous bubble cap according to claim 1, wherein: the full-mesh bubble cover comprises a round table-shaped micropore distribution full mesh constructed between a first supporting round table and a first upper round table, a small diameter end and a large diameter end of the micropore distribution full mesh are respectively connected with the first supporting round table and the first upper round table, the axes of the small diameter end and the large diameter end are coincident with each other, a first connecting sleeve extends on the first supporting round table along the axis of the first connecting sleeve in a direction away from the first upper round table, and the first connecting sleeve is detachably connected with the tower plate.
3. A novel tray with microporous bubble cap according to claim 2, wherein: the aperture of the micropore distribution whole net is 10-300 mu m, the diameter ranges of the first supporting round table and the first upper round table are 10-100 mm, the ratio of the height of the whole net type bubble cover to the height of the first supporting round table is 0.5-4, and the angle between the bevel edge of the micropore distribution whole net and the end face of the first supporting round table is 0-180 degrees.
4. A novel tray with microporous bubble cap according to claim 1, wherein: the half-mesh bubble cover comprises a round table-shaped micropore distribution half-mesh constructed between a second supporting round table and a second upper round table, a small diameter end and a large diameter end of the micropore distribution half-mesh are respectively connected with the second supporting round table and the second upper round table, the axes of the small diameter end and the large diameter end are coincident with each other, a second connecting sleeve extends on the second supporting round table along the axis of the second supporting round table in a direction away from the second upper round table, and the second connecting sleeve is detachably connected with the tower plate.
5. The novel tray with microporous bubble cap according to claim 4, wherein: the aperture of the micropore distribution half-net is 10-300 mu m, the diameter ranges of the second supporting round table and the second upper round table are both 10-100 mm, the ratio of the height of the half-net type bubble cover to the height of the second supporting round table is 0.5-4, and the angle between the bevel edge of the micropore distribution half-net and the end face of the second supporting round table is 0-180 degrees.
6. A novel tray with microporous bubble cap according to claim 1, wherein: the whole-net type air bubble cap arranged at the liquid inlet end of the tower plate is 0.5-5 mm higher than the whole-net type air bubble cap arranged at the overflow weir end.
7. A novel tray with microporous bubble cap according to claim 1, wherein: the full-mesh type air bubble caps are arranged in a regular triangle, and the distance between every two adjacent full-mesh type air bubble caps is 30-120 mm.
8. A novel tray with microporous bubble cap according to claim 1, wherein: the included angles between the central lines of the half-mesh type bubble caps and the central line of the overflow weir are 38 degrees, 48 degrees and 62 degrees respectively.
9. A novel tray with microporous bubble cap according to claim 1, wherein: the novel tower plates with the microporous bubble caps are arranged at intervals along the flow direction of the gas in the tower body, and the distance between the adjacent tower plates is 200-600mm.
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| CN110652943B (en) * | 2019-10-29 | 2020-09-22 | 浙江新安化工集团股份有限公司 | Bubble column reactor |
| CN111013178B (en) * | 2019-12-17 | 2021-06-22 | 浙江大学 | A stepped liquid loop bubble tower and method for dispersing gas |
| CN112973614A (en) * | 2021-02-10 | 2021-06-18 | 中国科学院过程工程研究所 | Gas-liquid reaction device, and use method and application thereof |
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| CN112973613A (en) * | 2021-02-10 | 2021-06-18 | 中国科学院过程工程研究所 | Continuous gas-liquid reaction system device and preparation method for continuously synthesizing tetrahydrophthalic anhydride by adopting same |
| CN118576999B (en) * | 2024-08-05 | 2024-11-08 | 河北金牛旭阳化工有限公司 | Adjustable plate type rectifying tower suitable for methanol production |
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| CN110354523A (en) | 2019-10-22 |
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