CN113941221B - Three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas - Google Patents
Three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas Download PDFInfo
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- CN113941221B CN113941221B CN202111462153.4A CN202111462153A CN113941221B CN 113941221 B CN113941221 B CN 113941221B CN 202111462153 A CN202111462153 A CN 202111462153A CN 113941221 B CN113941221 B CN 113941221B
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- 239000003546 flue gas Substances 0.000 title claims abstract description 57
- 238000000926 separation method Methods 0.000 title claims abstract description 41
- 239000000428 dust Substances 0.000 title claims abstract description 34
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 19
- 230000023556 desulfurization Effects 0.000 title claims abstract description 19
- 238000000746 purification Methods 0.000 title claims abstract description 12
- 238000001179 sorption measurement Methods 0.000 claims abstract description 17
- 238000001914 filtration Methods 0.000 claims abstract description 3
- 239000000463 material Substances 0.000 claims description 17
- 239000004964 aerogel Substances 0.000 claims description 16
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- 230000008901 benefit Effects 0.000 abstract description 4
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- 238000004581 coalescence Methods 0.000 abstract description 3
- 230000008878 coupling Effects 0.000 abstract description 2
- 238000010168 coupling process Methods 0.000 abstract description 2
- 238000005859 coupling reaction Methods 0.000 abstract description 2
- 230000003009 desulfurizing effect Effects 0.000 abstract 1
- 239000000779 smoke Substances 0.000 description 16
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- 239000002245 particle Substances 0.000 description 11
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Classifications
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
- B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
-
- 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
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/30—Physical properties of adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- General Chemical & Material Sciences (AREA)
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Abstract
The utility model relates to the technical field of flue gas treatment equipment, in particular to a three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas. The device consists of a hollow cylinder, a cylinder body formed by a reverse cone communicated with the lower end of the cylinder, a combined overflow pipe with a spiral blade and a filling cavity, a filtering module and a porous umbrella plate with a liquid collecting pipe, wherein the porous umbrella plate can move up and down. Through multidimensional coupling of solid-phase cyclone separation, liquid-phase coalescence separation and gas-phase adsorption separation, entrainment of three-phase pollutants in the flue gas can be effectively prevented, and integrated advanced treatment of efficient dust removal, liquid removal and desulfurization of the flue gas is realized. Can replace the prior multistage combined flue gas dust-removing, liquid-removing and desulfurizing device system, greatly reduces the deep treatment difficulty and the multi-aspect cost of the dust-containing and liquid-containing flue gas, and has considerable economic benefit.
Description
Technical Field
The utility model relates to a three-phase cyclone separation device for deep desulfurization and evolution of dust-containing liquid-containing flue gas. Technical field of flue gas treatment equipment
Technical Field
At present, the economy of China is continuously developed, the industrialization process is further accelerated, the atmospheric pollution situation is increasingly serious, the emission problem of smoke pollutants is more serious, smoke dust particles mixed in industrial smoke are the culprit and the first cause of severe weather such as haze, sand storm and the like, entrained micro liquid drops such as polycyclic aromatic hydrocarbon, nitroaromatic hydrocarbon and tar are the main causes of acid mist sedimentation in pollution sources and surrounding areas, and SO coexisting with the smoke 2 、NO X Gaseous pollutants such as benzene series and the like not only can harm animal, plant and human health, but also can cause light pollution, acid rain, ozone layer cavity and other environmental problems. Therefore, industrial flue gas pollution has become a great resistance for preventing the sustainable healthy development of the economic society in China.
The cyclone separation is a field separation method for separating two phases by utilizing cyclone centrifugal force based on two-phase density difference, belongs to the physical separation technology of heterogeneous systems, is commonly used for separating and classifying fine particles, and has the advantages of large treatment capacity, compact structure, simplicity and convenience in operation and the like. The cyclone is a high-efficiency unit device for realizing multiphase system separation by utilizing a cyclone separation technology. However, the conventional cyclone can only realize the two-phase separation of gas-solid, liquid-solid and gas-liquid with larger density difference under the restriction of turbulent diffusion and the influence of fluid phase state difference, and a multistage cyclone separation device is required to be connected in series in the practical industrial flue gas treatment application to realize flue gas dust removal and liquid removal.
Aerogels are solid materials with the highest known porosity and have the characteristics of low density, high specific surface area, large adsorption capacity, self-supporting adjustable pore structure, good mechanical properties and the like. The aerogel material with special wettability is applied in the oil-water two-phase separation process, and can effectively prevent water phase or oil phase substances from invading into the aerogel material by virtue of the super-hydrophobic or super-oleophobic characteristic of the surface of the aerogel material. Meanwhile, the active adsorption sites contained in the aerogel material can well capture free pollutant molecules or ions in the medium, so that the pollutant molecules or ions can be effectively separated. Therefore, the porous aerogel material with special wetting characteristics and excellent adsorption performance has great potential in industrial water treatment, deep purification of flue gas and other applications.
Chinese patent (CN 104958959B) discloses a multistage cyclone gas liquid removal method and a liquid remover. The utility model realizes the liquid removal treatment of the subsequent discharged flue gas by connecting the multi-stage cyclones in series up and down and utilizing hydrophilic liquid coalescent materials arranged on the inner wall and the rotating blades in each stage of cyclone in combination with the wet flue gas desulfurization device. However, the device can not replace the preamble flue gas purifying device, only can realize gas-liquid separation, and has no property of removing solid particles and gaseous pollutants in flue gas. In addition, the device occupies a large area and has high input cost.
Chinese patent utility models (CN 201720036227.0 and CN 200820102558.0) respectively disclose an inertial cyclone dust collector and a high-efficiency energy-saving cyclone dust collector. In both patents, a cylinder structure of a hollow cylinder with a reverse cone is adopted, a spiral baffle is arranged in a flue gas outlet to intercept fine particles in flue gas, and the effect of flue gas dust removal is realized. However, the device has single use and is only limited to flue gas dust removal. In addition, in the actual use process, the deep treatment of the dust-containing liquid-containing flue gas can be realized by matching with other flue gas treatment devices.
Disclosure of Invention
The utility model aims to solve the problems of large system occupation area, low separation efficiency, serious solid-liquid phase entrainment phenomenon and the like of the existing dust-containing liquid-containing flue gas advanced treatment device, and provides a novel flue gas dust-removing liquid-removing desulfurization integrated treatment device which has the advantages of compact structure, high separation efficiency, convenience in maintenance, no need of additional power input, no addition of any chemical reagent and the like.
The utility model has the following ideas:
the dust-containing liquid-containing flue gas is usually treated in a combined treatment mode, namely, the separation treatment of gas-solid, gas-liquid and pollutants in gas (gas state) is sequentially realized step by step according to the separation difficulty, different adsorption materials are adopted according to the treatment requirement of certain composite polluted flue gas in the treatment process, and special separation equipment is developed, so that a specific treatment process is formed, the cost is high, and the universality is poor.
The utility model aims at the smoke containing three-phase pollutants with different physicochemical properties, and realizes the integrated advanced treatment of high-efficiency dust removal, liquid removal and desulfurization of the smoke through multidimensional coupling of solid-phase cyclone separation, liquid-phase coalescence separation and gas-phase adsorption separation. Specifically:
1. the dust-containing liquid-containing flue gas enters the three-phase cyclone separation device from the tangential inlet, the cyclone component with the inverted cone structure forces the gas-liquid-solid three-phase fluid to generate strong rotary motion, and the gas-liquid-solid three-phase has different dynamic characteristics under the coupling action of the cyclone field and the gravity field due to the density and the size difference, is endowed with different migration speeds and displacements, and realizes rearrangement and layering of particle phases with different properties. The heavy phase dust particles are transferred to the peripheral wall surface of the component by means of a large centrifugal force, are firstly separated from the three-phase fluid, and are collected by the bottom flow port of the three-phase cyclone separation device.
2. The flue gas containing liquid migrates into the negative pressure zone in the central area of the three-phase cyclone separation device and moves upwards along with the internal rotational flow direction into the I-stage overflow pipe in the combined overflow pipe. The spiral blade in the I-stage overflow pipe forces micro-droplets with smaller density and fine granularity in the liquid-containing flue gas to collide and aggregate by strengthening the high-speed rotation movement of gas-liquid two-phase fluid in the internal rotational flow. In the process of rising along with the internal rotational flow, the micro-droplets enter a filling cavity connected with the two-stage overflow pipe through a porous umbrella plate arranged at the upper section of the I-stage overflow pipe.
3. The filler cavity is filled with porous aerogel adsorption material with specific wetting characteristics, and micro liquid drops cannot enter the aerogel adsorption material due to the special surface interface wetting property, are blocked on the outer surface of the material, further aggregate and grow up, are collected along the inclined surface to the central axis, and then drop into a liquid collecting pipeline coaxially arranged at the lower end of the porous umbrella plate and the I-stage overflow pipe channel, and are separated by a bottom flow port of the three-phase cyclone separation device.
4. The flue gas enters the porous aerogel adsorption material to move upwards after the flue gas is subjected to liquid removal, gaseous sulfide pollutants in the flue gas are adsorbed and separated by the porous aerogel filler, and finally purified flue gas subjected to dust removal, liquid removal and desulfurization is discharged from the upper end of the class II overflow pipe after the rectification effect of the porous umbrella plate and the porous aerogel adsorption material.
In summary, the three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas can realize rapid, stable and efficient flue gas dust removal, liquid removal and desulfurization.
The utility model is realized by the following technical scheme:
a three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas, which is characterized by comprising:
the combined overflow pipe penetrates through the baffle plate and stretches into the cylinder body; the combined overflow pipe comprises a lower-layer I-level overflow pipe with spiral blades, an upper-layer II-level overflow pipe and a filling cavity connected with the two-level overflow pipe, wherein the filling cavity is positioned on the upper side of the partition plate, a filter module is placed in the filling cavity, a porous umbrella plate with a liquid collecting pipe capable of moving up and down is arranged on the lower part of the filter module, and all parts of components in the combined overflow pipe are coaxial with the cylinder.
The length-diameter ratio L/D of the barrel body of the three-phase cyclone separation device is 2-10, and the cone angle alpha is 10-60 degrees.
Length L of class I overflow pipe in the combined overflow pipe of the utility model 2 Length L of cylindrical section of cylinder body 1 1/2-1 of diameter D 1 Is 1/4-1/3 of the diameter D of the cylinder. The spiral blade is arranged in the I-stage overflow pipe, the rotation direction is opposite to the rotation direction of the tangential inlet of the cylindrical section of the cylinder body, and the adjacent spiral blades are spaced by delta d 1 Length L of I-level overflow pipe 2 1/10-1/4 of the distance Deltad between the edges of the spiral blades and the liquid collection tube 2 1/2-1 of the diameter d of the liquid collection tube.
Length L of class II overflow tube in the combined overflow tube of the utility model 3 Length L of cylindrical section of cylinder body 1 1/4-1/2, class II overflow tube diameter D 2 Is the diameter D of the filling cavity 0 1/2 to 4/5 of the total weight of the composition.
In the combined overflow pipe, a filling cavity connecting a lower-layer I-level overflow pipe and an upper-layer II-level overflow pipe is a hollow cylinder and a cylinder body formed by a reverse cone communicated with the lower end of the cylinderLength-diameter ratio L 0 /D 0 1/2-2 of the diameter D of the filling cavity 0 1/2-2 of the diameter D of the cylinder, and the cone angle alpha of the conical section of the packing cavity 0 100-140 deg.. The filler cavity is positioned on the upper side of the partition board, and the distance H between the lower end surface of the filler cavity and the partition board is smaller than or equal to the length L of the cylindrical section of the cylinder body 1 1/10 of (C).
The filter module is a porous aerogel adsorption material with super-hydrophobic or super-oleophobic characteristic.
The porous umbrella plate and the liquid collecting pipe in the filling cavity in the combined overflow pipe are coaxial with the filling cavity, and the diameter D of the top of the porous umbrella plate 3 Is the diameter D of the filling cavity 0 3/5-4/5 of the cone angle alpha of the bottom end of the porous umbrella plate 1 80-160 degrees, the aperture ratio is 30-70 percent, and the diameter phi of the opening is 1-10mm. Length L of liquid collecting pipe 4 The length L of the cylindrical section of the cylinder body is greater than or equal to 1 The diameter D of the liquid collecting pipe is 1/16-1/12 of the diameter D of the cylinder.
Advantageous effects
According to the utility model, by integrating cyclone separation, coalescence separation and adsorption separation technologies, the cyclone fluid movement characteristic, the filter module surface interface wetting characteristic and the adsorption characteristic are utilized in a limited space, and meanwhile, the high-efficiency deep separation of three-phase pollutants (solid-phase smoke particles, liquid-phase micro-droplets and gas-phase sulfides) in the flue gas is realized. The device has compact structure, simple manufacturing process and convenient maintenance, does not need to additionally arrange a power input device or add any chemical reagent, and can be directly assembled at the tail end of a flue gas pipeline to replace a multi-stage combined flue gas dust removal liquid removal desulfurization device system. Compared with the prior art, the method greatly reduces the deep treatment difficulty and various costs of the dust-containing liquid-containing flue gas, and has considerable economic benefits.
Drawings
The accompanying drawings are included to provide a further understanding of the utility model, and are incorporated in and constitute a part of this specification.
In the drawings, the various elements are not necessarily drawn to scale.
FIG. 1 is a schematic diagram of the device of the present utility model.
Fig. 2 is an overall assembly view of the device of the present utility model.
FIG. 3 is a schematic view of the structural dimensions of the cartridge of the device of the present utility model.
FIG. 4 is a schematic view of the structural dimensions of the assembled overflow pipe of the device of the present utility model.
FIG. 5 is a schematic illustration of the structure of a porous umbrella plate with a liquid collection tube for the device of the present utility model.
Fig. 6 is a schematic three-dimensional structure of the device of the present utility model.
FIG. 7 is a schematic three-dimensional structure of a porous umbrella plate with a liquid collection tube in the device of the utility model.
Wherein reference numerals denote the following means and internals, respectively:
1: class II overflow tube, 2: packing cavity, 3: filtration module, 4: porous umbrella plate, 5: separator, 6: class I overflow tube, 7: helical blade, 8: tangential inlet, 9: cylindrical section, 10: liquid collection tube, 11: conical section, 12: and a bottom flow port.
Detailed Description
The utility model will be further described with reference to the drawings and specific examples. It is to be understood, however, that these examples are illustrative of the present utility model and are not to be construed as limiting the scope of the present utility model. The test methods in the following examples, in which specific conditions are not specified, are generally conducted under conventional conditions or under conditions recommended by the manufacturer. All percentages and parts are by weight unless otherwise indicated.
Example 1:
the device of the utility model is adopted in a certain heat-engine plant in Shanxi province to separate three-phase pollutants in the flue gas discharged by the existing thermal power generation boiler, and the flow rate of the flue gas is 20000m 3 And/h, the content of solid-phase smoke particles in the smoke is about 90-100mg/m 3 The polycyclic aromatic hydrocarbon content is about 50-80mg/m 3 Sulfur dioxide content of about 80-90mg/m 3 。
Design parameters: the three-phase cyclone separation device is assembled according to the figure 2, wherein the length-diameter ratio L/D of the cylinder body is 8, the cone angle alpha is 10 DEG, and the length L of the I-level overflow pipe in the combined overflow pipe 2 Length L of cylindrical section of cylinder body 1 3/4 of the diameter D 1 Is 1/3 of the diameter D of the cylinder. Adjacent helical blade spacing Δd 1 1/8 of the length L2 of the class I overflow pipe, the distance Deltad between the edge of the spiral blade and the liquid collecting pipe 2 1/2 of the diameter d of the liquid collection tube. Length L of class II overflow pipe 3 Length L of cylindrical section of cylinder body 1 Diameter D of class II overflow pipe 2 Is the diameter D of the filling cavity 0 1/2 of (C). Aspect ratio L of filler cavity 0 /D 0 1/2 of the diameter D of the filling cavity 0 1/2 of the diameter D of the cylinder, the cone angle alpha of the conical section of the packing cavity 0 100 deg.. The distance H between the lower end surface of the filling cavity and the partition plate is the length L of the cylindrical section of the cylinder body 1 1/12 of (C). Diameter D of top of porous umbrella plate 3 Is the diameter D of the filling cavity 0 3/5 of the cone angle alpha of the bottom end of the porous umbrella plate 1 120 degrees, 80 percent of aperture ratio and 2mm of aperture diameter phi. Length L of liquid collecting pipe 4 Length L of cylindrical section of cylinder body 1 The diameter D of the liquid collecting pipe is 1/16 of the diameter D of the cylinder. The filter module is a porous aerogel adsorption material with super oleophobic property.
The application effect is as follows: after the treatment by the device provided by the utility model, the removal rate of solid-phase smoke dust particles in the flue gas of the coal-fired boiler reaches 99%, the removal rate of polycyclic aromatic hydrocarbon reaches 98%, and the removal rate of sulfur dioxide reaches 97%.
Example 2:
the device of the utility model is adopted by a boiler plant in Zhejiang province to separate three-phase pollutants in the flue gas of the oil-fired boiler, and the flow rate of the flue gas is 22000m 3 And/h, the content of solid-phase smoke particles in the smoke is about 80-90mg/m 3 The polycyclic aromatic hydrocarbon content is about 40-60mg/m 3 Sulfur dioxide content of about 120-150mg/m 3 。
Design parameters: the three-phase cyclone separation device is assembled according to the figure 2, wherein the length-diameter ratio L/D of the cylinder body is 6, the cone angle alpha is 20 DEG, and the length L of the I-level overflow pipe in the combined overflow pipe 2 Length L of cylindrical section of cylinder body 1 1/2 of the diameter D 1 Is 1/4 of the diameter D of the cylinder. Adjacent helical blade spacing Δd 1 Length L of I-level overflow pipe 2 1/6 of the distance from the edge of the helical blade to the liquidSpacing Deltad of collection tubes 2 3/4 of the diameter d of the liquid collection tube. Length L of class II overflow pipe 3 Length L of cylindrical section of cylinder body 1 1/3 of the diameter D of the class II overflow pipe 2 Is the diameter D of the filling cavity 0 3/4 of (C). Aspect ratio L of filler cavity 0 /D 0 1, diameter D of packing cavity 0 2/3 of the diameter D of the cylinder body, and the cone angle alpha of the conical section of the packing cavity 0 Is 120 deg.. The distance H between the lower end surface of the filling cavity and the partition plate is the length L of the cylindrical section of the cylinder body 1 1/10 of (C). Diameter D of top of porous umbrella plate 3 Is the diameter D of the filling cavity 0 3/5 of the cone angle alpha of the bottom end of the porous umbrella plate 1 140 degrees, 60 percent of aperture ratio and 1mm of aperture diameter phi. Length L of liquid collecting pipe 4 Length L of cylindrical section of cylinder body 1 The diameter D of the liquid collecting pipe is 1/14 of the diameter D of the cylinder. The filter module is a porous aerogel adsorption material with super oleophobic property.
The application effect is as follows: after the treatment by the device provided by the utility model, the removal rate of solid-phase smoke dust particles in the flue gas of the oil-fired boiler reaches 98%, the removal rate of polycyclic aromatic hydrocarbon reaches 99%, and the removal rate of sulfur dioxide reaches 95%.
Example 3:
the device of the utility model is adopted in a coking plant in Hebei province to separate three-phase pollutants in dust-containing liquid-containing flue gas, and the flow rate of the flue gas is 18000m 3 And/h, the content of solid-phase smoke particles in the smoke is about 60-80mg/m 3 The polycyclic aromatic hydrocarbon content is about 80-100mg/m 3 Sulfur dioxide content of about 60-80mg/m 3 。
Design parameters: the three-phase cyclone separation device is assembled according to the figure 2, wherein the length-diameter ratio L/D of the cylinder body is 6, the cone angle alpha is 40 DEG, and the length L of the I-level overflow pipe in the combined overflow pipe 2 Length L of cylindrical section of cylinder body 1 2/3 of the diameter D 1 Is 1/3 of the diameter D of the cylinder. Adjacent helical blade spacing Δd 1 Length L of I-level overflow pipe 2 1/4 of the distance Deltad of the edges of the spiral blades from the liquid collection tube 2 4/5 of the diameter d of the liquid collection tube. Length L of class II overflow pipe 3 Length L of cylindrical section of cylinder body 1 Diameter D of class II overflow pipe 2 Is the diameter D of the filling cavity 0 4/5 of (C). Aspect ratio L of filler cavity 0 /D 0 2, diameter of packing cavity D 0 1.5 times of the diameter D of the cylinder body, and the cone angle alpha of the conical section of the packing cavity 0 Is 80 deg.. The distance H between the lower end surface of the filling cavity and the partition plate is the length L of the cylindrical section of the cylinder body 1 1/15 of (C). Diameter D of top of porous umbrella plate 3 Is the diameter D of the filling cavity 0 4/5 of the cone angle alpha of the bottom end of the porous umbrella plate 1 100 degrees, 40 percent of aperture ratio and 3mm of aperture diameter phi. Length L of liquid collecting pipe 4 Length L of cylindrical section of cylinder body 1 The diameter D of the liquid collecting pipe is 1/12 of the diameter D of the cylinder. The filter module is a porous aerogel adsorption material with super oleophobic property.
The application effect is as follows: after the treatment by the device provided by the utility model, the removal rate of solid-phase smoke dust particles in the coke oven flue gas reaches 99%, the removal rate of polycyclic aromatic hydrocarbon reaches 99%, and the removal rate of sulfur dioxide reaches 96%.
Claims (6)
1. A three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas, which is characterized by comprising:
the combined overflow pipe penetrates through the baffle plate and stretches into the cylinder body; the combined overflow pipe comprises a lower-layer I-level overflow pipe with spiral blades, an upper-layer II-level overflow pipe and a filling cavity connected with the two-level overflow pipe, wherein the filling cavity is positioned on the upper side of the partition plate, a filter module is placed in the filling cavity, a porous umbrella plate with a liquid collecting pipe capable of moving up and down is arranged on the lower part of the filter module, and all parts of components in the combined overflow pipe are coaxial with the cylinder.
2. The three-phase cyclone separation device for deep desulfurization purification of dust-containing liquid-containing flue gas according to claim 1, wherein the length-diameter ratio of the device cylinder is equal to that of the device cylinderL/DFrom 2 to 10, cone angleαIs 10-60 deg..
3. As claimed inThe three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas according to claim 1, wherein the length of the I-stage overflow pipe in the combined overflow pipe is as followsL 2 Length of cylindrical section of cylinderL 1 1/2-1 of the diameterD 1 Is the diameter of the cylinder bodyD1/4 to 1/3 of the total weight of the composition; the spiral blade is arranged in the I-stage overflow pipe, the rotation direction is opposite to the rotation direction of the tangential inlet of the cylindrical section of the cylinder body, and the interval between adjacent spiral blades is deltad 1 Length of class I overflow pipeL 2 1/10-1/4 of the distance of the edges of the spiral blades from the liquid collection tube is deltad 2 Diameter of liquid collecting piped1/2-1 of (C).
4. The three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas according to claim 1, wherein the combined overflow pipe has a class II overflow pipe lengthL 3 Length of cylindrical section of cylinderL 1 1/4-1/2, class II overflow tube diameterD 2 Is the diameter of the filling cavityD 0 1/2 to 4/5 of the total weight of the composition.
5. The three-phase cyclone separator for deep desulfurization and purification of dust-containing liquid-containing flue gas according to claim 1, wherein the filler cavity is a hollow cylinder and a cylinder body formed by a reverse cone communicated with the lower end of the cylinder, and the length-diameter ratio is thatL 0 /D 0 1/2-2 of the diameter of the filling cavityD 0 Is the diameter of the cylinder bodyD1/2-2 of the cone angle of the conical section of the packing cavityα 0 100-140 degrees; distance from lower end face of packing cavity to partition plateHIs less than or equal to the length of the cylindrical section of the barrel bodyL 1 1/10 of (C).
6. The three-phase cyclone separation device for deep desulfurization and purification of dust-containing liquid-containing flue gas according to claim 1, wherein the filtering module is a porous aerogel adsorption material with super-hydrophobic or super-oleophobic characteristics.
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| EP0659462A1 (en) * | 1993-12-22 | 1995-06-28 | FINMECCANICA S.p.A. AZIENDA ANSALDO | A system for hot dedusting flue gas from incinerators and thermal stations |
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| CN105126525A (en) * | 2015-09-24 | 2015-12-09 | 中国石油大学(华东) | Efficient vortex coalescing separator for gas purification |
| CN109276988A (en) * | 2018-10-25 | 2019-01-29 | 中国石油化工股份有限公司 | A kind of dust removal integrated method and apparatus of desulphurization denitration |
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| EP0659462A1 (en) * | 1993-12-22 | 1995-06-28 | FINMECCANICA S.p.A. AZIENDA ANSALDO | A system for hot dedusting flue gas from incinerators and thermal stations |
| CN104971575A (en) * | 2014-04-09 | 2015-10-14 | 苏州鼎德电环保科技有限公司 | Gas-liquid-solid separator, gas-liquid separator and plasma desulfurization and denitrification device comprising gas-liquid-solid separator and gas-liquid separator |
| WO2015154687A1 (en) * | 2014-04-09 | 2015-10-15 | 苏州鼎德电环保科技有限公司 | Gas-liquid-solid separator, gas-liquid separator and plasma desulphuration and denitration apparatus comprising same |
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