CN110935267A - Venturi tube and application thereof - Google Patents
Venturi tube and application thereof Download PDFInfo
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- CN110935267A CN110935267A CN201811114305.XA CN201811114305A CN110935267A CN 110935267 A CN110935267 A CN 110935267A CN 201811114305 A CN201811114305 A CN 201811114305A CN 110935267 A CN110935267 A CN 110935267A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/10—Venturi scrubbers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/30—Injector mixers
- B01F25/31—Injector mixers in conduits or tubes through which the main component flows
- B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/30—Injector mixers
- B01F25/31—Injector mixers in conduits or tubes through which the main component flows
- B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
- B01F25/3125—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof characteristics of the Venturi parts
- B01F25/31252—Nozzles
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Abstract
The invention discloses a Venturi tube and application thereof, wherein the Venturi tube comprises an outer cylinder, an inner cylinder and a plurality of groups of liquid phase nozzles which are arranged in parallel to the axial direction; the outer cylinder comprises a contraction section, a throat pipe I and a diffusion section I, the inner cylinder comprises a throat pipe II and a diffusion section II, the inner cylinder is positioned in the diffusion section I of the outer cylinder, an annular space is formed between the inner cylinder and the diffusion section, and the outer cylinder and the inner cylinder are preferably arranged coaxially; each group of nozzles comprises two liquid phase nozzles with opposite nozzle directions, and the liquid phase nozzles are respectively arranged at the tail end of the contraction section of the outer cylinder and the starting end of the diffusion section II of the inner cylinder; the initial end of the outer cylinder contraction section is a gas phase inlet, the tail end of the outer cylinder diffusion section I is a gas-liquid outlet, the liquid phase inlet is arranged on the pipe wall of the contraction section and/or the diffusion section, and the liquid phase inlet is communicated with the liquid phase nozzle through a liquid phase pipeline. The Venturi tube has good application prospect in the gas-liquid mass transfer process, and is particularly suitable for the fields of gas dust removal, such as flue gas desulfurization, flue gas dust removal, temperature reduction and the like.
Description
Technical Field
The invention belongs to the field of waste gas treatment, and particularly relates to a Venturi tube and application thereof.
Background
The venturi scrubber is also called venturi deduster and consists of a venturi tube and a demister. The dust removing process can be divided into three stages of atomization, condensation and demisting, the first two stages are carried out in a Venturi tube, and the last stage is finished in a demister. The venturi tube includes a converging section, a throat, and a diverging section. After the dust-containing gas enters the contraction section, the flow velocity is gradually increased along with the reduction of the pipe diameter and reaches the maximum value when entering the throat pipe. The washing liquid is generally added from a contraction section or a throat, the relative flow rate between gas phase and liquid phase is large, liquid drops are atomized under the action of high-speed airflow, the humidity of the gas reaches saturation, and dust particles in the gas are wetted by the washing liquid. After entering the diffusion section, the gas-liquid speed is reduced, the condensation action taking dust particles as condensation nuclei is accelerated, the dust particles are mutually bonded and condensed into dust-containing liquid drops with larger diameters and easy removal, and then the dust drops are captured in the demister.
The structure of the Venturi tube has various types, and the Venturi tube is divided into a round shape and a square shape according to the shape of a cross section; the adjustable and fixed are divided according to the adjustability of the diameter of the throat pipe; the method is divided into a forced type and a self-suction type according to the introduction mode of the washing liquid; the water supply method is divided into radial water spraying, axial water spraying and overflow water supplying. But in general, the combination of a venturi tube and an atomizing nozzle is simple, and two types are more commonly used: a kind of scrubber which adopts a bowl-shaped nozzle, the nozzle is arranged at the inlet of a Venturi tube and sprays water mist with a large diffusion angle to the downstream, when the scrubber of the type processes gas with high solid impurity content or viscous and easily agglomerated impurities, the scrubbed gas is easy to form re-entrainment or form adhesion on the wall surface; the other type adopts a radial water spraying type, a nozzle is positioned at the throat part, and water mist is sprayed out in the radial direction, and the scrubber of the type is more suitable for absorbing water-soluble gas impurities and has poor effect on gas containing solid impurities.
CN200964404Y discloses a venturi scrubber, which is modified by the structural characteristics of a hydraulic jet pump, and is designed with a special central feeding pipe structure. The special central feeding pipe structure forms a flowing form similar to a hydraulic jet pump, improves the washing effect of the washer on solid impurities and gaseous impurities, and has obvious effect on preventing secondary entrainment of washed gas and adhesion of impurity mucus. The venturi scrubber has the advantages that the power water nozzle discharges water from the front section to form jet flow, the size is large, the jet flow is not easy to separate into liquid drops in gas for atomization due to certain viscosity among liquid molecules, gas-liquid mixing is uneven, and gas scrubbing efficiency is reduced.
CN104208969A discloses a Venturi scrubber, which comprises a gas-liquid inlet, a gas-liquid spray hole, a washing section with a Venturi structure and a gas-liquid outlet; the gas-liquid inlet is provided with a gas-liquid spray hole, and the spraying direction of the liquid and the gas flow direction form a clockwise oblique angle of 156 degrees; the venturi structure scrubbing section has a convergent tube, a neck tube and a diffuser tube.
Can be used for cooling, dust removal and atomization, and has simple structure and low cost. However, the high-speed water flow in the venturi scrubber has large impact on the reducer pipe of the venturi structure, and the contraction pipe is easy to scale, so that the liquid spray holes are blocked, and the washing effect is influenced.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides the venturi tube which is simple in structure and good in gas-liquid mixing effect, has a good application prospect in the gas-liquid mass transfer process, and is particularly suitable for the fields of gas dust removal, such as flue gas desulfurization, flue gas dust removal, cooling and the like.
The Venturi tube comprises an outer cylinder, an inner cylinder and a plurality of groups of liquid phase nozzles arranged in parallel to the axial direction; the outer cylinder comprises a contraction section, a throat pipe I and a diffusion section I, the inner cylinder comprises a throat pipe II and a diffusion section II, the inner cylinder is positioned in the diffusion section I of the outer cylinder, an annular space is formed between the inner cylinder and the diffusion section, and the outer cylinder and the inner cylinder are preferably arranged coaxially; each group of nozzles comprises two liquid phase nozzles with opposite nozzle directions, and the liquid phase nozzles are respectively arranged at the tail end of the contraction section of the outer cylinder and the starting end of the diffusion section II of the inner cylinder; the initial end of the outer cylinder contraction section is a gas phase inlet, the tail end of the outer cylinder diffusion section I is a gas-liquid outlet, the liquid phase inlet is arranged on the pipe wall of the contraction section and/or the diffusion section, and the liquid phase inlet is communicated with the liquid phase nozzle through a liquid phase pipeline.
The names of the 'diffusion sections' of the inner barrel are unified according to the structural characteristics similar to or the same as those of the outer barrel, the diffusion sections of the inner barrel do not represent that the functions of the diffusion sections are similar to or the same as those of the diffusion sections of the outer barrel, and the specific functions need to be determined by combining practical application.
In the invention, one group of liquid phase nozzles is preferably arranged along the axial direction of the central shaft of the Venturi tube in the plurality of groups of liquid phase nozzles; preferably, 1-3 groups of liquid phase nozzles are arranged.
In the invention, the vertical distance between each group of liquid phase nozzles is 0.5-3 times, preferably 1-2 times of the length of the throat pipe I.
In the invention, the length ratio of the contraction section, the throat pipe I and the diffusion section I of the outer cylinder in the axial direction is 1-6: 1: 1 to 6.
In the invention, the axial length ratio of the diffusion section II of the inner cylinder to the throat pipe II is 1-10: 1.
the venturi tube is preferably provided with a straight tube section before the outer tube contraction section and/or after the outer tube diffusion section I, and the straight tube section can be connected with pipelines at the front and the rear of the venturi scrubber through flange connection or welding to play a role in rectification, so that the gas entering and exiting the venturi tube is concentrated in direction and distributed uniformly.
The taper angle α of the outer cylinder contraction section is 3-85 degrees, preferably 5-60 degrees, the taper angle β of the outer cylinder diffusion section I is 3-85 degrees, preferably 5-60 degrees, and the taper angle α of the outer cylinder contraction section is more preferably 0-5 degrees than the taper angle β of the outer cylinder diffusion section I.
The cone angle theta of the inner cylinder diffusion section II is 3-85 degrees, preferably 5-60 degrees, and the cone angle theta of the inner cylinder diffusion section II is more preferably 0-5 degrees smaller than the cone angle β of the outer cylinder diffusion section I.
The section of the throat pipe I can be in the shape of a circle, a square, a rectangle, an ellipse and the like, preferably is a circular section, and the diameter of the circular section is 10-2000 mm, preferably 20-1000 mm. The length of the throat pipe I is 1-3 times, preferably 1-2 times of the equivalent diameter of the throat pipe I.
The section of the throat pipe II is preferably the same as that of the throat pipe I in shape, and the equivalent diameter of the section of the throat pipe II is 0.4-0.5 times, preferably 0.5 times of that of the section of the throat pipe I. The length of the throat pipe II is 1-3 times, preferably 1-2 times of the equivalent diameter of the throat pipe II.
The inner cylinder is fixedly connected with the outer cylinder through connecting pieces, and the number of the connecting pieces is two or more, and the connecting pieces are arranged symmetrically along the circumferential direction.
In the invention, the liquid phase nozzle can be provided with one or more openings, the aperture of a single hole is 2-50 mm, the ratio of the total opening area of each liquid phase nozzle to the sectional area of the throat is 0.1-0.4, the openings of the nozzles are preferably uniformly distributed, and the angle of the opening of the nozzle is 30-150 degrees.
The application of the venturi tube in gas-liquid mass transfer comprises the following specific processes: liquid enters from a liquid phase inlet of the Venturi tube and is simultaneously and reversely sprayed out through the opposite liquid phase nozzles, violent impact is generated in the outer tube throat tube I along the axial direction, and an impact liquid level distributed along the radial direction is formed; meanwhile, gas enters the shrinkage section of the outer barrel from the gas phase inlet, the speed is gradually increased along with the reduction of the pipe diameter, the gas is fully contacted and atomized with the impact liquid surface in the throat pipe I, and the gas and the liquid are preliminarily mixed; the material flow after preliminary mixing flows through the annular space between the diffusion section I and the inner cylinder, one part of the material flow is discharged from a gas-liquid outlet, the other part of the material flow flows back to the inner cylinder under the action of pressure difference and reversely passes through the diffusion section II and the throat pipe II in sequence, the mixture atomized in the throat pipe II enters the throat pipe I, is contacted with the impact liquid level again, is atomized and mixed, enters the annular space between the diffusion section I and the inner cylinder together with the material flow after preliminary mixing, and the reflux process is continuously repeated.
In the process, after the liquid is reversely sprayed out through the liquid phase nozzle, the liquid drops are broken under the actions of extrusion, shearing and the like in the impact process of the liquid, the surfaces of the liquid drops are continuously updated, the contact area between the liquid drops and the gas is greatly increased, and the gas-liquid mass transfer efficiency is improved. The cross section of the outer tube throat pipe I is small, the liquid flow rate is high, and the impact force is large, so that the liquid is impacted in the outer tube throat pipe I to form a full-section diffusion impact surface distributed along the radial direction, and the diffusion impact surface basically maintains dynamic stability under continuous violent impact of two high-speed countercurrent liquid. Because the diffusion striking face of urceolus choke I department is full cross-section distribution, and the diffusion striking face keeps dynamic stability constantly renewing, and gas and liquid can both fully contact in whole urceolus choke I cross-section, simultaneously because the relative velocity of liquid and gas is higher, and the liquid drop atomizes rapidly under the impact of high velocity air, and gas-liquid is preliminary mixed. Part of the liquid phase nozzle is positioned in the inner cylinder diffusion section II, and because the liquid flow velocity of the liquid phase nozzle jet orifice is extremely high, the gas near the liquid phase nozzle is driven to flow at high speed together, the pressure energy of the gas near the liquid phase nozzle is converted into kinetic energy, the pressure of the area near the liquid phase nozzle is reduced, so that part of material flow after primary mixing is sucked into the inner cylinder diffusion section II under the action of pressure difference, then the part of material flow enters the inner cylinder throat II together with the high-speed liquid sprayed by the liquid phase nozzle, the atomization is carried out again at the position of the inner cylinder throat II, the gas and the liquid are further fully mixed, the mixture after the secondary atomization enters the throat I and is contacted with the impact liquid level again, the mixture is fully mixed and atomized, and enters the annular space between the diffusion section I and the inner cylinder together with the material flow after primary.
The liquid pressure flowing through the liquid phase nozzle is 0.1-0.6 MPa, and the ratio of the liquid flow rate to the inlet gas flow rate is 0.2-5, and the unit is L/Nm3。
The application of the venturi tube in gas dust removal comprises the following specific processes: liquid enters from a liquid phase inlet of the Venturi tube and is simultaneously and reversely sprayed out through the opposite liquid phase nozzles, violent impact is generated in the outer tube throat tube I along the axial direction, and an impact liquid level distributed along the radial direction is formed; meanwhile, the dust-containing gas enters the shrinkage section of the outer barrel from the gas phase inlet, the speed is gradually increased along with the reduction of the pipe diameter, the dust-containing gas is fully contacted and atomized with the impact liquid surface in the throat pipe I, and the gas and the liquid are fully mixed initially; the material flow after preliminary mixing flows through the annular space between the diffusion section I and the inner cylinder, one part of the material flow is discharged from a gas-liquid outlet, the other part of the material flow flows back to the inner cylinder under the action of pressure difference and reversely passes through the diffusion section II and the throat pipe II in sequence, the mixture atomized in the throat pipe II enters the throat pipe I, is contacted with the impact liquid level again, is atomized and mixed, enters the annular space between the diffusion section I and the inner cylinder together with the material flow after preliminary mixing, and the reflux process is continuously repeated. The dust particles carried by the gas are fully soaked by the liquid, and the dust particles are mutually bonded and agglomerated into particles with larger diameters, and are collected in a subsequent demister after being discharged from the diffusion section.
In the process, after the liquid is reversely sprayed out through the liquid phase nozzle, the liquid drops are broken under the actions of extrusion, shearing and the like in the impact process of the liquid, the surfaces of the liquid drops are continuously updated, the contact area between the liquid drops and the gas is greatly increased, and the gas-liquid mass transfer efficiency or the desulfurization efficiency is improved. The cross section of the outer tube throat pipe I is small, the liquid flow rate is high, and the impact force is large, so that the liquid is impacted in the outer tube throat pipe I to form a full-section diffusion impact surface distributed along the radial direction, and the diffusion impact surface basically maintains dynamic stability under continuous violent impact of two high-speed countercurrent liquid. Because the diffusion striking face of urceolus choke I department is full cross-section distribution, and the diffusion face keeps the dynamic stability constantly to be renewed, dusty gas can both fully contact with liquid in whole urceolus choke I cross-section, simultaneously because the relative velocity of liquid and gas is higher, has realized that the liquid drop carries the initiative collision of granule to gas, and the liquid drop atomizes rapidly under the impact of high velocity air, and gas-liquid is preliminary mixed. Part of the liquid phase nozzle is positioned in the inner cylinder diffusion section II, and because the liquid flow velocity of the liquid phase nozzle jet orifice is extremely high, the gas near the liquid phase nozzle is driven to flow at high speed, the pressure energy of the gas near the liquid phase nozzle is converted into kinetic energy, the pressure of the area near the liquid phase nozzle is reduced, so that part of material flow after primary mixing is sucked into the inner cylinder diffusion section II under the action of pressure difference, then the part of material flow enters the inner cylinder throat II together with the high-speed liquid sprayed by the liquid phase nozzle, the atomization is carried out again at the inner cylinder throat II, the gas and the liquid are further fully mixed, the mixture after the secondary atomization enters the throat I and is contacted with the impact liquid level again, the full mixing and the atomization are carried out, the material flow after primary mixing enters the annular space between the diffusion section I and the inner cylinder together, the backflow process is repeated continuously, dust particles carried by the gas are fully soaked, the dust particles are mutually bonded and agglomerated into particles with larger diameters, and are easier to be captured in a subsequent demister, secondary entrainment of side flow, wall flow or washed gas is avoided, and efficient flue gas dust removal is realized.
Compared with the prior art, the Venturi tube has the following advantages:
1. according to the invention, the liquid phase nozzle is arranged in the Venturi tube, after the liquid flows out of the nozzle, violent impact is generated in the throat tube I along the axial direction, and the liquid generates the actions of extrusion, shearing and the like in the impact process to break liquid drops, so that the surfaces of the liquid drops are continuously updated, and the contact area between the liquid drops and gas is greatly increased. The liquid is impacted in the throat pipe I to form a radially distributed full-section diffusion impact surface, the diffusion impact surface is distributed in a full-section mode, and gas and liquid drops can be fully contacted in the whole section of the throat pipe I. The diffusion impact surface basically maintains dynamic stability under the action of continuous and violent impact of two high-speed liquids, the relative speed of liquid drops and gas is high, the liquid drops are quickly atomized under the impact of high-speed gas flow, and the gas and the liquid are preliminarily mixed; the material flow after the preliminary mixing flows through the annular space, one part of material flow is discharged from a gas-liquid outlet, the other part of material flow flows back to the inner cylinder under the action of pressure difference, reversely passes through the diffusion section II and the throat pipe II in sequence, the mixture atomized in the throat pipe II enters the throat pipe I, is contacted with the impact liquid level again, is atomized and mixed, enters the annular space between the diffusion section I and the inner cylinder together with the material flow after the preliminary mixing, and the backflow process is continuously repeated.
2. The volume is small, the occupied space is small, and the cost is low; the structure is simple, the manufacture is convenient, the blockage and the scaling are not easy to occur, the impact on the structure is small, and the long-term stable operation can be realized;
3. the ratio of the liquid flow rate to the gas flow rate is 0.2 to 5 (unit is L/Nm)3) The device is particularly suitable for the condition of small liquid-gas ratio, and can save water.
Drawings
FIG. 1 is a schematic diagram of the venturi tube with a straight section according to the present invention.
FIG. 2 is a schematic diagram of the venturi tube without a straight section according to the present invention.
FIG. 3 is a schematic structural diagram of the outer cylinder of the venturi tube of the present invention.
FIG. 4 is a schematic structural view of the inner cylinder of the venturi tube of the present invention.
FIG. 5 is a schematic diagram of a conventional axial water jet venturi.
In the figure, 1-outer cylinder, 2-gas phase inlet, 3-gas-liquid outlet, 4-liquid phase inlet, 5-liquid phase pipeline, 6-liquid phase nozzle, 7-connecting piece, 8-inner cylinder.
Wherein, 1-straight section, 1-2-contraction section, 1-3-throat I, 1-4-diffusion section I, 8-1-throat II, 8-2-diffusion section II.
Detailed Description
The Venturi tube comprises an outer cylinder 1, an inner cylinder 8 and a plurality of groups of liquid phase nozzles 6 which are arranged in parallel to the axial direction; the outer cylinder 1 comprises a contraction section 1-2, a throat pipe I1-3 and a diffusion section I1-4, the inner cylinder 8 comprises a throat pipe II8-1 and a diffusion section II8-2, the inner cylinder 8 is positioned in the diffusion section I1-4 of the outer cylinder 1, an annular space is formed between the inner cylinder 8 and the diffusion section, and the outer cylinder 1 and the inner cylinder 8 are preferably arranged coaxially; each group of nozzles comprises two liquid phase nozzles 6 with opposite nozzle directions, and the two liquid phase nozzles are respectively arranged at the tail end of a contraction section 1-2 of the outer cylinder 1 and the starting end of a diffusion section II8-2 of the inner cylinder 8; the initial end of the contraction section 1-2 of the outer cylinder 1 is a gas phase inlet 2, the tail end of the diffusion section I1-4 of the outer cylinder 1 is a gas-liquid outlet 3, the liquid phase inlet 4 is arranged on the pipe wall of the contraction section 1-2 and/or the diffusion section, and the liquid phase inlet 4 is communicated with the liquid phase nozzle 6 through a liquid phase pipeline 5.
The designation of the 'diffuser' of the inner cylinder 8 in the invention is unified according to the structural features similar or identical to those of the outer cylinder 1, and the diffuser of the inner cylinder 8 does not represent that the function is similar or identical to that of the diffuser of the outer cylinder 1, and the specific function needs to be determined by combining practical application.
In the invention, one group of liquid phase nozzles 6 is preferably arranged along the axial direction of the central shaft of the Venturi tube in the plurality of groups of liquid phase nozzles 6; preferably, 1 to 3 sets of liquid phase nozzles 6 are provided.
In the invention, the vertical distance between each group of liquid phase nozzles 6 is 0.5-3 times, preferably 1-2 times of the length of the throat I1-3.
In the invention, the length ratio of the contraction section 1-2, the throat pipe I1-3 and the diffusion section I1-4 of the outer cylinder 1 in the axial direction is 1-6: 1: 1 to 6.
In the invention, the axial length ratio of the diffuser section II8-2 of the inner cylinder 8 to the throat pipe II8-1 is 1-10: 1.
the venturi tube of the invention is preferably provided with a straight tube section 1-1 before the contraction section 1-2 of the outer tube 1 and/or after the diffusion section I1-4 of the outer tube 1, the straight tube section 1-1 can be connected with the front and rear pipelines of the venturi scrubber through flange connection or welding to play a role in rectification, so that the gas entering and exiting the venturi tube is more concentrated and distributed more uniformly.
The taper angle α of the contraction section 1-2 of the outer cylinder 1 is 3-85, preferably 5-60, the taper angle β of the diffusion section I1-4 of the outer cylinder 1 is 3-85, preferably 5-60, and the taper angle α of the contraction section 1-2 of the outer cylinder 1 is equal to the taper angle β of the diffusion section I1-4 of the outer cylinder 1 or 0-5 larger than the taper angle β of the diffusion section I1-4 of the outer cylinder 1.
The cone angle theta of the inner cylinder 8 diffusion section II8-2 is 3-85, preferably 5-60, and the cone angle theta of the inner cylinder 8 diffusion section II8-2 is more preferably equal to the cone angle β of the outer cylinder 1 diffusion section I1-4 or 0-5 less than the cone angle β of the outer cylinder 1 diffusion section I1-4.
The section of the throat I1-3 can be in the shape of a circle, a square, a rectangle, an ellipse and the like, preferably is a circular section, and the diameter of the circular section is 10-2000 mm, preferably 20-1000 mm. The length of the throat I1-3 is 1-3 times, preferably 1-2 times of the equivalent diameter of the throat I1-3.
The section of the throat II8-1 is preferably the same as the section of the throat I1-3 in shape, and the equivalent diameter of the section of the throat II8-1 is 0.4-0.5 times, preferably 0.5 times of the equivalent diameter of the section of the throat I1-3. The length of the throat pipe II8-1 is 1-3 times, preferably 1-2 times of the equivalent diameter of the throat pipe II 8-1.
The inner cylinder 8 is fixedly connected with the outer cylinder 1 through connecting pieces 7, and the number of the connecting pieces 7 is two or more and is arranged symmetrically along the circumferential direction.
In the invention, the liquid phase nozzle 6 can have one or more openings, the aperture of a single hole is 2-50 mm, the ratio of the total opening area of each liquid phase nozzle 6 to the sectional area of the throat is 0.1-0.4, the openings of the nozzles are preferably uniformly distributed, and the angle of the opening of the nozzle is 30-150 degrees.
The liquid pressure flowing through the liquid phase nozzle 6 is 0.1-0.6 MPa, and the ratio of the liquid flow rate to the inlet gas flow rate is 0.2-5, and the unit is L/Nm 3.
Example 1
The Venturi tube with the structure shown in the figure 1 is applied to flue gas dust removal, and the flue gas flow is 80Nm3H, dust content 300g/m3. The diameter of the outer cylinder throat in the Venturi tube is 30mm, the length of the outer cylinder throat is 60mm, the taper angles of the outer cylinder contraction section and the outer cylinder diffusion section are both 20 degrees, the lengths of the outer cylinder contraction section and the outer cylinder diffusion section are both 60mm, and the lengths of the outer cylinder inlet and outlet straight cylinder sections are both 20 mm. The diameter of the throat of the inner cylinder is 15mm, the length of the throat of the inner cylinder is 30mm, the length of the contraction section of the inner cylinder is 30mm, and the cone angle of the contraction section of the inner cylinder is 20 degrees. A group of nozzles are axially arranged in the Venturi tube, the vertical distance between the two nozzles is 40mm, the opening aperture on each nozzle is 15mm, the ratio of the total opening area of each nozzle to the sectional area of the throat is 0.25, and the opening angle is 90 degrees. The ratio of the liquid flow rate to the flue gas flow rate is 0.2 to 5 (L/Nm)3) After being washed by the Venturi tube and treated by the subsequent wire mesh demister, the dust content of the flue gas is reduced by 98.8 percent.
Comparative example 1
In the same way as in example 1, in a conventional axial water-spraying venturi tube, the diameter of the throat is 30mm, the length of the throat is 60mm, the taper angles of the contraction section and the diffusion section are both 20 degrees, the lengths of the contraction section and the diffusion section are both 60mm, and the lengths of the inlet and outlet straight tube sections are both 20 mm. A single nozzle is axially arranged in the contraction section of the Venturi tube, the aperture of an opening on the nozzle is 15mm, the ratio of the total opening area on the nozzle to the sectional area of the throat tube is 0.25, and the opening angle is 90 degrees. The ratio of the liquid flow rate to the flue gas flow rate is 0.2-5 (L/Nm)3) Under the condition of washing by a conventional axial water spraying Venturi tube shown in figure 3 and demisting by a subsequent silk screenAfter the treatment of the device, the dust content of the smoke is reduced by 80 percent.
Example 2
The Venturi tube of the invention shown in figure 2 is applied to flue gas desulfurization, and the flue gas flow is 80000Nm3H, SO in flue gas2Has a concentration of 980mg/m3. The diameter of the outer barrel throat in the Venturi tube is 1000mm, the length of the outer barrel throat is 1500mm, the taper angle of the outer barrel contraction section and the taper angle of the outer barrel diffusion section are both 10 degrees, and the length of the outer barrel contraction section and the length of the outer barrel diffusion section are both 2000 mm. The diameter of the throat of the inner cylinder is 500mm, the length of the throat of the inner cylinder is 750mm, the length of the contraction section of the inner cylinder is 1000mm, and the cone angle of the contraction section of the inner cylinder is 20 degrees. A group of nozzles are axially arranged in the Venturi tube, the vertical distance between the two nozzles is 2000mm, the aperture on each nozzle is 30mm, the ratio of the total opening area of each group of nozzles to the sectional area of the throat is 0.3, and the opening angle is 80-100 degrees. The ratio of the liquid flow rate to the flue gas flow rate is 0.2 to 5 (L/Nm)3) After being washed by the Venturi tube and treated by a subsequent demister, SO in the flue gas2Has a concentration of 10mg/m3。
Comparative example 2
In the same way as in example 2, in a conventional axial water-spraying venturi tube, the diameter of a throat in the venturi tube is 1000mm, the length of the throat is 1500mm, the taper angles of a contraction section and a diffusion section are both 10 degrees, and the lengths of the contraction section and the diffusion section are both 2000 mm. A single nozzle is arranged in the venturi tube along the axial direction, the aperture of the opening on the nozzle is 30mm, the ratio of the total opening area on the nozzle to the sectional area of the throat tube is 0.3, and the opening angle is 80-100 degrees. The ratio of the liquid flow rate to the flue gas flow rate is 0.2-5 (L/Nm)3) Under the condition, after being washed by the conventional axial water spraying Venturi tube shown in figure 3 and treated by the subsequent demister, SO in the flue gas2Has a concentration of 50mg/m3。
Example 3
The venturi of figure 1 of the present invention is applied to the production of alkylated gasoline wherein the gas is 80Nm3C of/h4Alkane and olefin mixture, liquid is 98% concentrated sulfuric acid, the concentrated sulfuric acid is used as catalyst, and C is reacted at 10 deg.c4Preparation of alkane and olefin by alkylation reactionA high octane gasoline component. The diameter of the outer cylinder throat in the Venturi tube is 30mm, the length of the outer cylinder throat is 60mm, the taper angles of the outer cylinder contraction section and the outer cylinder diffusion section are both 20 degrees, the lengths of the outer cylinder contraction section and the outer cylinder diffusion section are both 60mm, and the lengths of the outer cylinder inlet and outlet straight cylinder sections are both 20 mm. The diameter of the throat of the inner cylinder is 15mm, the length of the throat of the inner cylinder is 30mm, the length of the contraction section of the inner cylinder is 30mm, and the cone angle of the contraction section of the inner cylinder is 20 degrees. A group of nozzles are axially arranged in the Venturi tube, the vertical distance between the two nozzles is 30mm, the aperture on each nozzle is 15mm, the ratio of the total opening area on each nozzle to the sectional area of the throat is 0.25, and the opening angle is 90 degrees. The ratio of the liquid flow rate to the flue gas flow rate is 1 to 1.5 (L/Nm)3) After the mixing by the Venturi tube, the conversion rate of the olefin is more than 80 percent.
Comparative example 3
In the conventional axial water-spraying venturi tube shown in fig. 3, the diameter of the throat in the venturi tube is 30mm, the length of the throat is 60mm, the taper angles of the contraction section and the diffusion section are both 20 °, the lengths of the contraction section and the diffusion section are both 60mm, and the lengths of the inlet and outlet straight tube sections are both 20 mm. A single nozzle is axially arranged in the Venturi tube, the aperture of an opening on the nozzle is 15mm, the ratio of the total opening area on the nozzle to the sectional area of the throat is 0.25, and the opening angle is 90 degrees. In the production of alkylated gasoline, when the gas is 300Nm3C of/h4The alkane and olefin mixture is mixed with 98% concentrated sulfuric acid as liquid, the concentrated sulfuric acid is used as a catalyst, and the ratio of the liquid flow to the flue gas flow is 1-1.5 (L/Nm)3) After mixing with a conventional axial water jet venturi as shown in figure 3, the olefin conversion was about 65%.
Claims (16)
1. A venturi, characterized by: comprises an outer cylinder, an inner cylinder and a plurality of groups of liquid phase nozzles arranged in parallel to the axial direction; the outer cylinder comprises a contraction section, a throat pipe I and a diffusion section I, the inner cylinder comprises a throat pipe II and a diffusion section II, the inner cylinder is positioned in the diffusion section I of the outer cylinder, an annular space is formed between the inner cylinder and the diffusion section, and the outer cylinder and the inner cylinder are preferably arranged coaxially; each group of nozzles comprises two liquid phase nozzles with opposite nozzle directions, and the liquid phase nozzles are respectively arranged at the tail end of the contraction section of the outer cylinder and the starting end of the diffusion section II of the inner cylinder; the initial end of the outer cylinder contraction section is a gas phase inlet, the tail end of the outer cylinder diffusion section I is a gas-liquid outlet, the liquid phase inlet is arranged on the pipe wall of the contraction section and/or the diffusion section, and the liquid phase inlet is communicated with the liquid phase nozzle through a liquid phase pipeline.
2. The venturi of claim 1, wherein: and one of the liquid phase nozzles is axially arranged along the central shaft of the Venturi tube.
3. The venturi according to claim 1 or 2, wherein: 1-3 groups of liquid phase nozzles are arranged.
4. The venturi of claim 1, wherein: the vertical distance between each group of liquid phase nozzles is 0.5-3 times of the length of the throat pipe I.
5. The venturi of claim 1, wherein: the length ratio of the contraction section of the outer cylinder to the throat pipe I to the diffusion section I in the axial direction is 1-6: 1: 1 to 6.
6. The venturi of claim 1, wherein: the axial length ratio of the diffusion section II of the inner cylinder to the throat pipe II is 1-10: 1.
7. the venturi of claim 1, wherein: the straight cylinder section is arranged before the outer cylinder contraction section and/or after the outer cylinder diffusion section I.
8. The venturi tube of claim 1, wherein the taper angle α of the convergent section of the outer cylinder is 3-85 °, and the taper angle β of the divergent section I of the outer cylinder is 3-85 °.
9. The venturi of claim 8, wherein the taper angle α of the converging section of the outer barrel is 0-5 ° greater than the taper angle β of the diverging section I of the outer barrel.
10. The venturi of claim 1, wherein: the cone angle theta of the inner cylinder diffusion section II is 3-85 degrees.
11. The venturi of claim 1, wherein: the length of the throat pipe I is 1-3 times of the equivalent diameter of the throat pipe I.
12. The venturi of claim 1, wherein: the equivalent diameter of the section of the throat pipe II is 0.4-0.5 times of the equivalent diameter of the section of the throat pipe I; the length of the throat pipe II is 1-3 times of the equivalent diameter of the throat pipe II.
13. The venturi of claim 1, wherein: the liquid phase nozzle has one or more openings, the aperture of a single hole is 2-50 mm, the ratio of the total opening area of each liquid phase nozzle to the sectional area of the throat is 0.1-0.4, and the opening angle of the nozzle is 30-150 degrees.
14. The application of the Venturi tube of claim 1 in gas-liquid mass transfer is characterized by comprising the following specific steps: liquid enters from a liquid phase inlet of the Venturi tube and is simultaneously and reversely sprayed out through the opposite liquid phase nozzles, violent impact is generated in the outer tube throat tube I along the axial direction, and an impact liquid level distributed along the radial direction is formed; meanwhile, gas enters the shrinkage section of the outer barrel from the gas phase inlet, the speed is gradually increased along with the reduction of the pipe diameter, the gas is fully contacted and atomized with the impact liquid surface in the throat pipe I, and the gas and the liquid are preliminarily mixed; the material flow after preliminary mixing flows through the annular space between the diffusion section I and the inner cylinder, one part of the material flow is discharged from a gas-liquid outlet, the other part of the material flow flows back to the inner cylinder under the action of pressure difference and reversely passes through the diffusion section II and the throat pipe II in sequence, the mixture atomized in the throat pipe II enters the throat pipe I, is contacted with the impact liquid level again, is atomized and mixed, enters the annular space between the diffusion section I and the inner cylinder together with the material flow after preliminary mixing, and the reflux process is continuously repeated.
15. The application of the Venturi tube of claim 1 in gas dedusting is characterized by comprising the following specific steps: liquid enters from a liquid phase inlet of the Venturi tube and is simultaneously and reversely sprayed out through the opposite liquid phase nozzles, violent impact is generated in the outer tube throat tube I along the axial direction, and an impact liquid level distributed along the radial direction is formed; meanwhile, the dust-containing gas enters the shrinkage section of the outer barrel from the gas phase inlet, the speed is gradually increased along with the reduction of the pipe diameter, the dust-containing gas is fully contacted and atomized with the impact liquid surface in the throat pipe I, and the gas and the liquid are fully mixed initially; the material flow after preliminary mixing flows through the annular space between the diffusion section I and the inner cylinder, one part of the material flow is discharged from a gas-liquid outlet, the other part of the material flow flows back to the inner cylinder under the action of pressure difference and reversely passes through the diffusion section II and the throat pipe II in sequence, the mixture atomized in the throat pipe II enters the throat pipe I, is contacted with the impact liquid level again, is atomized and mixed, enters the annular space between the diffusion section I and the inner cylinder together with the material flow after preliminary mixing, and the reflux process is continuously repeated; the dust particles carried by the gas are fully soaked by the liquid, and the dust particles are mutually bonded and agglomerated into particles with larger diameters, and are collected in a subsequent demister after being discharged from the diffusion section.
16. Use according to claim 14 or 15, characterized in that: the liquid pressure flowing through the liquid phase nozzle is 0.1-0.6 MPa, the ratio of the liquid flow rate to the inlet gas flow rate is 0.2-5, and the unit is L/Nm3。
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| CN111905906A (en) * | 2020-07-29 | 2020-11-10 | 中国石油化工股份有限公司 | Centrifugal separation and mechanical crushing type coal dust cleaning system and working method thereof |
| CN113145007A (en) * | 2021-05-26 | 2021-07-23 | 昆明珑瑞一焰气体产品配送服务有限公司 | Device for mixed conveying of natural gas and additive |
| CN114542977A (en) * | 2022-02-28 | 2022-05-27 | 清华大学 | Natural gas hydrogen-mixing device |
| CN114700320A (en) * | 2022-02-23 | 2022-07-05 | 圣达电气有限公司 | Cleaning mechanism of copper foil raw foil machine |
| CN114748981A (en) * | 2022-03-24 | 2022-07-15 | 重庆众源盛特环保设备制造有限公司 | Active dynamic film generator |
| CN114849503A (en) * | 2022-07-07 | 2022-08-05 | 北京石油化工学院 | Air dissolving equipment |
| CN116237176A (en) * | 2023-05-11 | 2023-06-09 | 四川工程职业技术学院 | Built-in atomization device and built-in atomization method |
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| CN114849503A (en) * | 2022-07-07 | 2022-08-05 | 北京石油化工学院 | Air dissolving equipment |
| CN116237176A (en) * | 2023-05-11 | 2023-06-09 | 四川工程职业技术学院 | Built-in atomization device and built-in atomization method |
| CN116237176B (en) * | 2023-05-11 | 2023-07-25 | 四川工程职业技术学院 | Built-in atomization device and built-in atomization method |
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Effective date of registration: 20230922 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. |